AU2016266238B2 - Method for operating coal gasification system - Google Patents
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- AU2016266238B2 AU2016266238B2 AU2016266238A AU2016266238A AU2016266238B2 AU 2016266238 B2 AU2016266238 B2 AU 2016266238B2 AU 2016266238 A AU2016266238 A AU 2016266238A AU 2016266238 A AU2016266238 A AU 2016266238A AU 2016266238 B2 AU2016266238 B2 AU 2016266238B2
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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
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Abstract
Provided is a method for operating a coal gasification system (1) which manufactures at least hydrogen gas and carbon monoxide gas by allowing coal to be gasified using the coal gasification system (1) having a two-layer structured coal gasification reaction furnace (20) that includes: a partial oxidization unit (21) which is disposed on a bottom column and partially oxidizes coal; and a pyrolysis unit (22) which communicates with the partial oxidization unit (21), is disposed on a top column, and pyrolyzes the coal. In this method, coal and char are supplied to the partial oxidization unit (21) as well as supplied to the pyrolysis unit (22), and when the weight of ash increases, the amount of fixed carbon supplied into the pyrolysis unit (22) is also increased, said weight of the ash generated from the coal supplied to the partial oxidization unit (21) and is supplied to the pyrolysis unit.
Description
Technical Field] [0001]
The present invention relates to a method for operating a coal gasification system.
The present application claims priority on the basis of Japanese Patent
Application No. 2015-104747, filed in Japan on May 22, 2015, the content of which is incorporated herein by reference.
[Background Art] [0002]
Conventionally, coal gasification systems having entrained-flow, two-chamber, two-stage coal gasification reactors have been considered for the gasification of coal to produce hydrogen gas and carbon monoxide gas (see, e.g., Patent Documents 1 and 2).
Coal gasification reactors of this type have a partial oxidation portion that is provided in a lower stage and that partially oxidizes the coal, and a pyrolysis portion that is provided in an upper stage and that pyrolyzes the coal.
[0003]
Coal and oxygen (oxidizing agent) are loaded into the partial oxidation portion, which is the lower stage, and the coal is partially oxidized so as to gasify the coal.
Simultaneously with the gasification of the coal, slag (ash) contained in the coal melts.
The molten slag is drained outside the system through a slag tap disposed in a lower portion of the partial oxidation portion.
[Related Literature] [Patent Literature] [0004] [Patent Document 1]
Japanese Unexamined Patent Application, First Publication No. 2012-241105 [Patent Document 2]
Japanese Unexamined Patent Application, First Publication No. 2014-136764 [Summary of Invention] [Technical Problem] [0005]
A portion of the molten slag accompanies the gas and is scattered into the pyrolysis portion, which is the upper stage. At this time, slagging, in which scattered slag adhere inside the pyrolysis portion, may occur.
By blowing (feeding) coal into the pyrolysis portion of the coal gasification reactor, it is possible to capture (collect) the molten and scattered slag and to thereby prevent slagging to some degree. The coal that is blown into the pyrolysis portion is decomposed into volatile components and char by the sensible heat of the oxygen-free high-temperature gas that rises from the partial oxidation portion. The volatile components are recovered as gas, and the char functions as a capturing material for the ash scattered from the partial oxidation portion into the pyrolysis portion. In other words, of the coal that is blown into the pyrolysis portion, the char, which is the part that is left after removing the volatile components, is effective in capturing slag. However, with this method for preventing slagging, when using high-ash coal, in which the ash content, i.e., the ratio of the mass of the ash in the coal with respect to the mass of the coal, is at least 10%, which is increasingly becoming the object of gasification in recent years, the slag that is scattered from the partial oxidation portion increases, so the amount of coal that is blown into the pyrolysis portion must also be increased. The reactions undergone by coal in the pyrolysis portion are generally endothermic reactions. Thus, if the amount of coal blown into the pyrolysis portion is increased, then the temperature inside the pyrolysis portion will decrease, tar will be generated and the generated amount of pyrolysis gas will be insufficient.
[0006]
The pyrolysis portion in Patent Document 2 is provided with a water-cooled wall, so that the slag inside the pyrolysis portion is rapidly cooled at the wall surfaces and will not adhere on the wall surfaces.
The problem of slagging does not easily occur in the pyrolysis portion of Patent
Document 2 due to the fact that the structure of the coal gasification reactor differs from that of the coal gasification reactor of Patent Document 1, in which the pyrolysis portion has a refractory structure.
[0007]
The present invention was made in consideration of these problems, and has the purpose of providing a method for operating a coal gasification system wherein the adhesion of slag inside the pyrolysis portion is suppressed while limiting decreases in the temperature inside the pyrolysis portion.
[Solution to Problem] [0008]
The present invention proposes the following means in order to solve the above-mentioned problems.
In the method for operating a coal gasification system having a two-stage coal gasification reactor provided with a partial oxidation portion positioned at a lower stage, in which coal is partially oxidized, and a pyrolysis portion positioned at an upper stage along with communicating with the partial oxidation portion, in which coal is pyrolyzed, at least hydrogen gas and carbon monoxide gas are produced by gasifying coal in the coal gasification system. This method includes feeding coal and char into the partial oxidation portion and the pyrolysis portion. The amount of fixed carbon to be fed into the pyrolysis portion is increased when the weight of ash fed into the pyrolysis portion, that is generated from the coal in the partial oxidation portion, increases.
[0009]
Additionally, in the other method for operating a coal gasification system having a two-stage coal gasification reactor provided with a partial oxidation portion positioned at a lower stage, in which coal is partially oxidized, and a pyrolysis portion positioned at an upper stage along with communicating with the partial oxidation portion, in which coal is pyrolyzed, at least hydrogen gas and carbon monoxide gas are produced by gasifying coal in the coal gasification system. This method includes feeding coal and char into the partial oxidation portion and the pyrolysis portion. The weight of fixed carbon to be fed into the pyrolysis portion is increased in proportion to the weight of ash fed into the pyrolysis portion, that is generated from the coal in the partial oxidation portion.
[0010]
According to these inventions, ash in the coal fed into the partial oxidation portion is present as molten slag, and part of this slag rises from the inside of the partial oxidation portion to the inside of the pyrolysis portion.
Slagging is prevented by capturing the scattered molten slag with fixed carbon contained in coal and char. When char is loaded into the pyrolysis portion, since the volatile components have been eliminated from the char, the entire amount of the char that is loaded into the pyrolysis portion is effective as a capturing material. Therefore, compared to the case in which only coal, which includes volatile components, is blown into the pyrolysis portion, the amount of coal that is blown into the pyrolysis portion can be reduced, and temperature decreases in the pyrolysis portion can be suppressed.
Additionally, the reactions by which the volatile components are decomposed from coal to form char are generally endothermic. Therefore, temperature decreases in the pyrolysis portion can be suppressed in comparison to the case in which only coal is blown into the pyrolysis portion.
[0011]
Additionally, inside the partial oxidation portion, the volatile components are decomposed from the fed coal to form char. Furthermore, the fixed carbon contained in the char instantly gasifies, and the ash in the char becomes molten slag.
[Advantageous Effects of Invention] [0012]
In the present invention, according to the methods for operating a coal gasification system according to claims 1 and 2, it is possible to limit decreases in the temperature inside the pyrolysis portion due to the heat of vaporization that is lost to the volatile components. Additionally, since the char captures ash, the adhesion of slag inside the pyrolysis portion can be suppressed.
Additionally, even if the weight of ash fed into the pyrolysis portion increases, slag can still be captured by the fixed carbon, of which the amount that is fed into the pyrolysis portion is increased.
[Brief Description of Drawings] [0013]
Fig. 1 is a block diagram illustrating a coal gasification system according to an embodiment of the present invention.
Fig. 2 is a section view for explaining the operations in a coal gasification reactor in the coal gasification system.
Fig. 3 is a diagram showing fixed carbon that has captured slag in the coal gasification system according to an embodiment of the present invention.
Fig. 4 is a diagram showing the inside of a pyrolysis portion in which slagging has occurred in a coal gasification system according to a comparative example.
[Description of Embodiments] [0014]
Herebelow, an embodiment of the coal gasification system (hereinafter sometimes abbreviated to “system”) according to the present invention will be explained with reference to Fig. 1 to 4. Together with the explanation of the present system, the method for operating the system according to the present embodiment will also be described.
The system of the present embodiment is a plant installation that uses coal as a raw material and that gasifies the coal to produce hydrogen gas and carbon monoxide gas or the like.
As shown in Fig. 1, the system 1 in the present embodiment comprises a coal crusher & dryer 10, a bag filter 11, a coal feeding hopper 12, a lower-stage coal feeder 13, an upper-stage coal feeder 14, a coal gasification reactor 20, a heat recovery unit 25, a dust collector 26, char recovery equipment (char recovery apparatus) 27 and a char feeder (char feeding apparatus) 28.
[0015]
The system 1 of the present embodiment can be used with various types of coal, such as bituminous coal, sub-bituminous coal and lignite. The present system 1 can be favorably used not only with the aforementioned coal having an ash content of less than
10%, but also with high-ash coal having an ash content of 10% or more.
Generally, the outer diameter of coal is irregular, and bituminous coal, sub-bituminous coal and lignite contain large quantities, for example, about 10% to 60%, of moisture. Therefore, the coal is crushed and dried in the coal crusher & dryer 10.
The coal is crushed to a fine powder such that the outer diameter is, for example, at least about 10 pm (micrometers) and at most about 100 pm, and dried until the water content in the coal becomes, for example, 2% to 20%.
The coal that is crushed and dried in this way is fed to the bag filter 11 by being carried on a gas flow using carbon dioxide gas or the like as the carrier gas.
[0016]
The bag filter 11 is of a generally known structure. The bag filter 11 removes dust or the like contained in the fine powdered coal. The coal from which dust or the like has been removed by the bag filter 11 is fed to the coal feeding hopper 12.
The coal feeding hopper 12 stores coal inside thereof, and feeds the stored coal to the lower-stage coal feeder 13 and the upper-stage coal feeder 14.
The lower-stage coal feeder 13 feeds fine powdered coal, carried by a gas flow, to a gasification burner 21a, to be described below, in the coal gasification reactor 20.
Similarly, the upper-stage coal feeder 14 feeds fine powdered coal, carried by a gas flow, to a feed nozzle 22a, to be described below, in the coal gasification reactor 20.
[0017]
The coal gasification reactor 20 has a two-stage structure provided with a partial oxidation portion 21 positioned at a lower stage and a pyrolysis portion 22 positioned at an upper stage along with communicating with the partial oxidation portion 21. Below the partial oxidation portion 21, a slag-cooling water tank, not shown, which communicates with the partial oxidation portion 21, is provided.
The partial oxidation portion 21 and the pyrolysis portion 22 are reaction chambers, in each of which internal spaces, not shown, are formed. The internal space of the partial oxidation portion 21 and the internal space of the pyrolysis portion 22 are in communication with each other.
The partial oxidation portion 21, the pyrolysis portion 22 and the slag-cooling water tank are formed from heat-resistant refractory materials. A water-cooled wall (water-cooling apparatus) for cooling the partial oxidation portion 21 may be provided on the outer circumferential surface of the partial oxidation portion 21. In the present embodiment, the pyrolysis portion 22 is not provided with a water-cooled wall.
However, a water-cooled wall could be provided in the pyrolysis portion 22.
The partial oxidation portion 21 is provided with a gasification burner 21a and a char burner 21b. The gasification burner 21a and the char burner 21b form a first feeding portion 21c.
[0018]
In the operation method for the system 1, through the gasification burner 21a, coal from the lower-stage coal feeder 13, oxygen gas separated in an air separator, not shown, and steam generated by the heat recovery unit 25 are each fed (blown) into the partial oxidation portion 21. From the char burner 21b, char is fed into the partial oxidation portion 21. Char is fixed carbon (carbon components) obtained by decomposition of moisture and volatile components from coal. The char may contain ash.
[0019]
The fine powdered coal, char, oxygen gas and steam that are fed into the partial oxidation portion 21 rise while swirling inside the partial oxidation portion 21. At this time, the inside of the partial oxidation portion 21 is at a high temperature and a high pressure (for example, the temperature in the internal space in the partial oxidation portion 21 is at least 1250 °C and at most 1500 °C, and the pressure is at least 2 MPa (megapascals) and at most 5 MPa). In this environment, coal and char gasify to generate high-temperature carbon monoxide gas, carbon dioxide gas, hydrogen gas and slag (ash) based on the chemical reactions represented by the following formulas (1) to (4):
| 2C + O2 - | -+2CO | ...(1) | |
| C + O2^ | •CO2 | • · (2) | |
| C + H2O | -+ co + h2 | • · (3) | |
| 10 | C + CO2 - | -+2CO | • · (4) |
[0020]
The moisture and volatile components are decomposed from the coal fed into the partial oxidation portion 21, generating char. The char instantly gasifies and the ash contained in the char becomes molten slag.
The gas, char, slag and the like generated in the partial oxidation portion 21 rise while swirling inside the partial oxidation portion 21 and move into the pyrolysis portion
22. Fig. 2 shows the slag W1 moving from the inside of the partial oxidation portion 21 into the inside of the pyrolysis portion 22.
Some of the slag W1 generated inside the partial oxidation part 21 adhere on the inside surface of the partial oxidation portion 21 (see Fig. 2), slides along the wall of the coal gasification reactor 20, and falls into the water in the slag-cooling water tank, where it is cooled and recovered.
Inside the partial oxidation portion 21, the coal is partially oxidized in a state of incomplete combustion in which there is insufficient oxygen.
[0021]
As shown in Fig. 1, the pyrolysis portion 22 is provided with a feed nozzle 22a and a char feed nozzle 22b. The feed nozzle 22a and the char feed nozzle 22b form a second feeding portion 22c.
In the operation method for the system 1, coal is fed through the feed nozzle 22a into the pyrolysis portion 22. At the same time that coal is being fed into the pyrolysis portion 22, a defined amount of steam generated in the heat recovery unit 25 may be fed into the pyrolysis portion 22. Char is fed into the pyrolysis portion 22 from the char feed nozzle 22b.
In the present embodiment, the temperature in the internal space in the pyrolysis portion 22 is controlled so as to be at least 950 °C and at most 1100 °C (preferably approximately 1000 °C). If the temperature inside the pyrolysis portion 22 becomes lower than 950 °C, the amount of tar that is generated suddenly increases, and it becomes difficult for a tar decomposition reaction to occur inside the pyrolysis portion 22. At this temperature, the slag does not melt and is solid.
The carbon and steam contained in the coal that is fed into the pyrolysis portion reacts due to the chemical reaction represented by the above-indicated formula (3), and is decomposed into carbon monoxide gas and hydrogen gas.
Additionally, some of the carbon contained in the coal fed into the pyrolysis portion 22 reacts with the carbon dioxide gas inside the pyrolysis portion 22 and becomes carbon monoxide gas due to the chemical reaction represented by the above-indicated formula (4).
In this way, the coal undergoes pyrolysis inside the pyrolysis portion 22.
[0022]
Regarding the char that is fed from the char feed nozzle 22b into the pyrolysis portion 22, as shown in Fig. 2 and 3, the fixed carbon in the char W2 captures the slag
Wl.
Since the volatile components have been eliminated from the char, the entire amount of the char that is loaded into the pyrolysis portion 22 is effective as a capturing material. Therefore, compared to a comparative example in which only coal, which includes volatile components, is blown into the pyrolysis portion 22, the amount of the coal that is blown into the pyrolysis portion 22 can be reduced, and temperature decreases in the pyrolysis portion 22 can be suppressed.
In the method for operating the system 1, the weight of fixed carbon that is fed into the pyrolysis portion 22 by the coal and the char can be increased in proportion to the weight (mass) of the slag Wl fed into the pyrolysis portion 22, that is generated from the coal and the char in the partial oxidation portion 21. In other words, the weight of the fixed carbon that captures the slag W1 can be increased in proportion to the weight of the slag Wl that is fed to the pyrolysis portion 22.
[0023]
When char is not fed into the pyrolysis portion 22 from the char feed nozzle 22b indicated as a comparative example, the slag that is scattered inside the pyrolysis portion is not sufficiently captured. In this case, as shown in Fig. 4, slagging, in which slag
Wl adhere inside the pyrolysis portion 22, occurs. Fig. 4 shows the inside of the pyrolysis portion 22 seen from the side of the connecting portion between the partial oxidation portion 21 and the pyrolysis portion 22 in the coal gasification reactor of the comparative example.
In contrast therewith, with the system 1 and the method for operating the system according to the present embodiment, the slag that is scattered in the pyrolysis portion is captured by the char, thereby suppressing the adhesion of slag inside the pyrolysis 25 portion 22.
[0024]
Additionally, high-temperature generated gas comprising hydrogen gas, carbon monoxide gas, carbon dioxide gas and the like produced in the pyrolysis portion 22 is carried together with the char W2 that has captured the slag W1 and is fed to the heat recovery unit 25 shown in Fig. 1. The main components in the generated gas are carbon monoxide gas and hydrogen gas.
[0025]
In the heat recovery unit 25, the generated gas and char produced in the pyrolysis portion 22 are cooled by exchanging heat with coolant water and the coolant water becomes steam. A predetermined amount of the steam produced in the heat recovery unit 25 is fed to the partial oxidation portion 21 and the pyrolysis portion 22.
The generated gas and char that have been cooled in the heat recovery unit 25 are fed to the dust collector 26. The dust collector 26 has a cyclone structure, and the generated gas and char are centrifugally separated in the dust collector 26. The char recovery equipment 27 recovers the char collected in the dust collector 26. The char recovered in the char recovery equipment 27 is fed to the char feeder 28.
The char feeder 28 feeds char to the char burner 21b and the char feed nozzle
22b.
[0026]
On the other hand, the generated gas that has passed through the dust collector is fed to a shift reactor (not shown). Additionally, in order to raise the ratio of hydrogen gas with respect to carbon monoxide gas in the generated gas to a certain value, a predetermined amount of steam is fed to the generated gas before entering the shift reactor, and due to the shift reaction represented by the following chemical reaction formula (5), the carbon monoxide gas in the generated gas reacts with the steam to produce hydrogen gas and carbon dioxide gas.
CO + H2O CO2 + H2 ... (5) [0027]
The generated gas of which the components are adjusted in the shift reactor is fed to a gas cooler/gas purifier (not shown), and impurity component gases and the like, typically sulfur compounds, contained in the generated gas, are collected.
The generated gas that has passed through the gas cooler/gas purifier is carried to a downstream step to produce a synthesis gas such as methane or methanol.
[0028]
As explained above, according to the system 1 and the method for operating the system 1 of the present embodiment, the ash in the coal and the char fed into the partial oxidation portion 21 are present in a molten state, and a portion of this slag rises from the inside of the partial oxidation portion 21 to the inside of the pyrolysis portion 22.
However, this scattered slag is captured by the char, so the adhesion of slag inside the pyrolysis portion 22 can be suppressed.
By feeding (recycling) char inside the pyrolysis portion 22, fixed carbon that captures the slag is fed from the char, thereby allowing the amount of the coal fed into the pyrolysis portion 22 to be reduced.
[0029]
The slag adhering inside the pyrolysis portion is in the form of glass. In order to remove this slag from the pyrolysis portion, the operation of the system 1 is stopped once and the coal gasification reactor 20 is disassembled. Then, the slag that has been adhering inside the pyrolysis portion must be chipped away (scraped away). The work of chipping the slag away from the pyrolysis portion requires a period of, for example, several days.
While char will gasify inside the partial oxidation portion 21, which has a relatively high temperature, it will not gasify in the pyrolysis portion 22, which has a relatively low temperature. For this reason, even if char is fed into the pyrolysis portion
22, the char does not gasify, so the gasification efficiency is lowered. The gasification efficiency, as mentioned here, refers to the ratio of the calories in the hydrogen gas, carbon monoxide gas and the like that can be produced by the coal, with respect to the calories in the loaded coal.
However, by feeding char into the pyrolysis portion 22, it becomes less likely for slagging to occur in the pyrolysis portion 22, and the system 1 can be stably and continuously operated.
[0030]
The temperature inside the internal space in the partial oxidation portion 21 is at least 1250 °C and at most 1500 °C, and the temperature inside the internal space in the pyrolysis portion 22 is at least 950 °C and at most 1100 °C. For this reason, the generation of tar in the pyrolysis portion 22 can be suppressed while melting the slag in the partial oxidation portion 21.
The weight of the fixed carbon fed into the pyrolysis portion 22 is increased in proportion to the weight of slag fed into the pyrolysis portion 22. As a result, even if the weight of slag fed into the pyrolysis portion 22 is increased, the slag can be captured by the fixed carbon of which the amount fed into the pyrolysis portion 22 has been increased.
[0031]
While an embodiment of the present invention has been heretofore described in detail with reference to the drawings, the specific structure is not limited to this embodiment, and modifications, combinations and deletions of features and the like may be made within a range not departing from the gist of the present invention.
For example, in the aforementioned embodiment, the char recovered by the char recovery equipment 27 is fed by the char feeder 28 to the char burner 21b and the char feed nozzle 22b. However, the char recovered by the char recovery equipment 27 may be fed to the bag filter 11 by being carried by a gas flow or the like. In that case, the char is mixed into the coal in the coal feed hopper 12, and the coal mixed with the char is fed into the partial oxidation portion 21 and the pyrolysis portion 22 respectively by means of the lower-stage coal feeder 13 and the upper-stage coal feeder 14. A char feed nozzle 22b is not provided in the pyrolysis portion 22. The second feeding portion forms the feed nozzle 22a.
Due to this structure, it becomes unnecessary to provide a char feed nozzle 22b in the pyrolysis portion 22 in order to feed char into the pyrolysis portion 22, and the equipment of the system 1 can be simplified.
[0032] (Examples)
Herebelow, the present invention will be explained in further detail by specifically describing examples and comparative examples, but the present invention should not be construed as being limited to the following examples.
Coal having ash contents of 6%, 8%, 10% and 12% was used to perform tests of the examples and comparative examples of the present invention.
The total amount of coal and char fed (blown) into the pyrolysis portion 22, which is the upper stage, was adjusted to be approximately 200 kg/h (kilograms per hour)
The total amount of coal and char fed into the partial oxidation portion, which is the lower stage, was adjusted to be approximately 560 kg/h.
The amount (recycled amount) of char fed into the pyrolysis portion 22 was adjusted to be 0 kg/h (char not fed) or approximately 29 kg/h with respect to the ash content of the coal.
When the amount of char fed to the pyrolysis portion 22 was 0 kg/h, the amount of char fed to the partial oxidation portion 21 was set to approximately 80.5 kg/h.
When the amount of char fed into the pyrolysis portion 22 was approximately 29 kg/h, the amount of char fed into the partial oxidation portion 21 was set to approximately 52.0 kg/h.
Experiments were performed under Operating Conditions Nos. 1-8 shown in
Table 1, by using the two different amounts of char fed into the pyrolysis portion 22 with respect to the four different values for the ash content.
[0033] [Table 1]
| Operating Condition No. | Ash Content (%) | Amount of Coal and Char Fed into Pyrolysis Portion (Upper Stage) (kg/h) | Amount of Coal and Char Fed into Partial Oxidation Portion (Lower Stage) (kg/h) | Amount of Char Fed into Pyrolysis Portion (Upper Stage) (kg/h) | Amount of Char Fed into Partial Oxidation Portion (Lower Stage) (kg/h) | Slagging in Pyrolysis Portion (Adhesion) |
| 1 | 6 | 200.4 | 560.5 | 0.0 | 80.5 | Absent |
| 2 | 201.1 | 560.2 | 28.9 | 51.6 | absent | |
| 3 | 8 | 200.6 | 561.3 | 0.0 | 80.4 | absent |
| 4 | 199.5 | 560.2 | 28.6 | 51.8 | absent | |
| 5 | 10 | 201.1 | 559.9 | 0.0 | 80.6 | present |
| 6 | 200.3 | 560.2 | 28.9 | 51.7 | absent | |
| 7 | 12 | 200.5 | 560.4 | 0.0 | 80.1 | present |
| 8 | 200.1 | 560.2 | 28.6 | 51.5 | absent |
[0034]
For example, under Operating Condition No. 1, no char is fed into the pyrolysis portion 22. Thus, the amount of coal fed into the pyrolysis portion 22 is 200.4 kg/h, which is equal to the total amount of coal and char fed into the pyrolysis portion 22.
Under Operating Condition No. 2, the amount of char fed into the pyrolysis portion 22 is 28.9 kg/h. Therefore, the amount of coal fed into the pyrolysis portion 22 is 172.2 kg/h, which is 28.9 kg/h subtracted from 201.1 kg/h, the total amount of coal and char fed into the pyrolysis portion 22.
Operating Conditions Nos. 2, 4, 6 and 8, in which char is fed into the pyrolysis portion 22, are examples of the present invention. Operating Conditions Nos. 1, 3, 5 and 7, in which char is not fed into the pyrolysis portion 22, are comparative examples with respect to the present invention.
[0035]
For example, while the amount of coal fed into the pyrolysis portion 22 under
Operating Condition No. 1 is 200.4 kg/h, the amount of coal fed into the pyrolysis portion 22 under Operating Condition No. 2, in which char is fed into the pyrolysis portion 22, is 172.2 kg/h, so the amount is reduced from that under Operating Condition
No. 1.
This is because, under Operating Condition No. 2, it is possible to use not only the fixed carbon contained in the char fed into the pyrolysis portion 22, but also that in the coal fed into the pyrolysis portion 22, as the fixed carbon for capturing the slag.
Additionally, unless the amount of coal fed into the pyrolysis portion 22 is reduced, the temperature inside the pyrolysis portion 22 tends to become lower than 950 °C, in which case the amount of tar that is generated increases.
[0036]
Under Operating Conditions Nos. 2, 4, 6 and 8 in which char is fed into the pyrolysis portion 22, it was found that slagging does not occur in the pyrolysis portion 22 for any of the values for ash content of 6%, 8%, 10% and 12%. On the other hand, under Operating Conditions Nos. 1, 3, 5 and 7 in which char is not fed into the pyrolysis portion 22, it was found that slagging occurs when the ash content is 10% and 12%.
Thus, it was found that the coal gasification system and the method for operating a coal gasification system of the present embodiment can be used irrespective of the ash content of coal, but can be used particularly favorably with respect to coal having an ash content of 10% or more.
[Reference Signs List] [0037]
System (coal gasification system)
Coal gasification reactor
Partial oxidation portion
21c First feeding portion
Pyrolysis portion
22c Second feeding portion
2016266238 16 Oct 2018
Claims (3)
1/3
1. A method for operating a coal gasification system having a two-stage coal gasification reactor provided with a partial oxidation portion positioned at a lower stage, in which coal is partially oxidized, and a pyrolysis portion positioned at an upper stage along with communicating with the partial oxidation portion, in which coal is pyrolyzed, wherein at least hydrogen gas and carbon monoxide gas are produced by gasifying coal in the coal entrainedflow gasification system, the method comprising:
feeding coal and char into the partial oxidation portion and the pyrolysis portion, wherein the amount of fixed carbon contained in the coal and in the char to be fed into the pyrolysis portion is increased when the weight of ash fed into the pyrolysis portion, that is generated from the coal in the partial oxidation portion, increases.
2/3
FIG. 2
W1 W1
FIG. 3
2. A method for operating a coal gasification system having a two-stage coal gasification reactor provided with a partial oxidation portion positioned at a lower stage, in which coal is partially oxidized, and a pyrolysis portion positioned at an upper stage along with communicating with the partial oxidation portion, in which coal is pyrolyzed, wherein at least hydrogen gas and carbon monoxide gas are produced by gasifying coal in the entrained-flow coal gasification system, the method comprising:
feeding coal and char into the partial oxidation portion and the pyrolysis portion, wherein the weight of fixed carbon contained in the coal and in the char to be fed into the pyrolysis portion is increased in proportion to the weight of ash fed into the pyrolysis portion, that is generated from the coal in the partial oxidation portion.
Nippon Steel & Sumikin Engineering Co., Ltd.
Patent Attorneys for the Applicant/Nominated Person
SPRUSON & FERGUSON
21405296 (IRN: P279943)
FIG. 1
3/3
FIG. 4
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015-104747 | 2015-05-22 | ||
| JP2015104747A JP5816770B1 (en) | 2015-05-22 | 2015-05-22 | Operation method of coal gasification system |
| PCT/JP2016/063056 WO2016190028A1 (en) | 2015-05-22 | 2016-04-26 | Method for operating coal gasification system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2016266238A1 AU2016266238A1 (en) | 2017-10-05 |
| AU2016266238B2 true AU2016266238B2 (en) | 2018-11-08 |
Family
ID=54602117
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2016266238A Active AU2016266238B2 (en) | 2015-05-22 | 2016-04-26 | Method for operating coal gasification system |
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| JP (1) | JP5816770B1 (en) |
| CN (1) | CN107429176B (en) |
| AU (1) | AU2016266238B2 (en) |
| WO (1) | WO2016190028A1 (en) |
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| JP6637797B2 (en) * | 2016-03-11 | 2020-01-29 | 三菱日立パワーシステムズ株式会社 | Carbon-containing raw material gasification system and method for setting oxidizing agent distribution ratio |
| CN110804465A (en) * | 2019-11-20 | 2020-02-18 | 张俊霞 | Device and method for producing hydrogen by gasifying plastic biomass |
| CN112207121B (en) * | 2020-10-30 | 2023-11-21 | 南京师范大学 | Graded thermal purification method and device for incineration fly ash based on carbothermic reduction |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5450508A (en) * | 1977-09-30 | 1979-04-20 | Agency Of Ind Science & Technol | Gasification |
| US4168956A (en) * | 1977-08-18 | 1979-09-25 | Combustion Engineering, Inc. | Method of operating a coal gasifier |
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| JP2003105351A (en) * | 2001-09-28 | 2003-04-09 | Nippon Steel Corp | Method and apparatus for quick thermal decomposition of coal |
| AU2010246510B2 (en) * | 2009-12-01 | 2013-01-24 | Electric Power Development Co. Ltd. | Gasifier, thermal power plant using gasifier, operating procedure of gasifier, and operating procedure of thermal power plant using gasifier |
| JP5386635B2 (en) * | 2010-04-16 | 2014-01-15 | 新日鉄住金エンジニアリング株式会社 | Operation method of coal gasification reactor and coal gasification reactor |
| JP5639955B2 (en) * | 2011-05-19 | 2014-12-10 | 新日鉄住金エンジニアリング株式会社 | Coal gasification system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4168956A (en) * | 1977-08-18 | 1979-09-25 | Combustion Engineering, Inc. | Method of operating a coal gasifier |
| JPS5450508A (en) * | 1977-09-30 | 1979-04-20 | Agency Of Ind Science & Technol | Gasification |
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| Publication number | Publication date |
|---|---|
| AU2016266238A1 (en) | 2017-10-05 |
| WO2016190028A1 (en) | 2016-12-01 |
| JP5816770B1 (en) | 2015-11-18 |
| CN107429176B (en) | 2020-07-31 |
| CN107429176A (en) | 2017-12-01 |
| JP2016216649A (en) | 2016-12-22 |
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Owner name: NIPPON STEEL ENGINEERING CO., LTD. Free format text: FORMER NAME(S): NIPPON STEEL & SUMIKIN ENGINEERING CO., LTD. |