CN217733013U - Coal conversion device - Google Patents
Coal conversion device Download PDFInfo
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- CN217733013U CN217733013U CN202222112832.5U CN202222112832U CN217733013U CN 217733013 U CN217733013 U CN 217733013U CN 202222112832 U CN202222112832 U CN 202222112832U CN 217733013 U CN217733013 U CN 217733013U
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Abstract
The utility model relates to a coal conversion technical field, concretely relates to coal conversion device, including down gasification bed, go upward dry distillation bed, whirlwind dust removal unit, coal gas cooling unit and coal gas washing unit, its simple structure, reasonable in design can adopt the fine particle coal as the raw materials, through going upward dry distillation bed and down gasification bedCombining, namely converting coal step by step, firstly recovering volatile components in the coal through an ascending carbonization bed to obtain certain coal tar and carbonization gas, feeding the coal tar obtained by carbonization into a descending gasification bed, gasifying the coal tar at high temperature in the lower gasification bed to generate coal gas, and recovering the tar and methane in the coal gas, and then, recovering the rest of CO and H 2 As the synthesis raw material gas, the active ingredients in the coal can be converted and recovered to the maximum extent; it is suitable for light coal, and has low requirement for water content, ash content and composition in coal, and good conversion effect.
Description
Technical Field
The utility model relates to a coal conversion technical field especially relates to a coal conversion device.
Background
The energy resource characteristics of China are lean oil, lean gas and rich coal, and along with the requirement of double carbon, the efficient and clean utilization of coal becomes more important.
Currently, a variety of coal gasification plants are widely used, and these plants are characterized in that, for example, a fixed bed requires a large raw material and produces water containing phenol; if the entrained flow bed adopts the fine pulverized coal, the treatment capacity is high, but the requirements on the coal types are strict; the gasification furnace is very sensitive to the change of coal quality of coal types, and the reliability of production is influenced.
Therefore, there is a need for a new coal carbonization apparatus that reduces the restrictions on the types of raw materials and maximizes the conversion and recovery of the effective components of coal.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides a coal conversion device, its simple structure, reasonable in design requires lowly to the raw materials constitution, and coal conversion is effectual.
The utility model adopts the technical proposal that:
a coal conversion device comprises a descending gasification bed, an ascending carbonization bed, a cyclone dust removal unit, a coal gas cooling unit and a coal gas washing unit;
the top end of the descending gasification bed is provided with a gasification gas inlet and a gasification feed inlet, the gasification feed inlet is respectively connected with the cyclone dust removal unit and the coal gas washing unit, and the bottom end of the descending gasification bed is connected with the bottom end of the ascending carbonization bed;
the bottom end of the ascending dry distillation bed is provided with a dry distillation feed inlet, and the top end of the ascending dry distillation bed is connected with the cyclone dust removal unit;
the coal gas cooling unit is respectively connected with the cyclone dust removal unit and the coal gas washing unit.
In some embodiments, the downer gasification bed is configured as a downer spouted bed; the ascending carbonization bed is arranged as an ascending conveying bed.
In some embodiments, the middle lower end of the downward gasification bed is provided with a gasification agent inlet and a semicoke inlet, and the semicoke inlet is connected with the cyclone dust removal unit.
In some embodiments, the gasification device further comprises a combustor, and the gasification agent inlet and the semicoke inlet are respectively connected with the combustor.
In some embodiments, the cyclone dust removal unit is provided with a primary cyclone dust collector and a secondary cyclone dust collector which are connected with each other;
the primary cyclone dust collector is respectively connected with the top end of the ascending dry distillation bed, the gasification feed inlet and the semicoke inlet;
and the secondary cyclone dust collector is respectively connected with the coal gas cooling unit and the semicoke inlet.
In some embodiments, the primary cyclone is provided with a first dipleg for storing coarse semicoke, and the first dipleg is respectively connected with the gasification feed inlet and the semicoke inlet;
and the secondary cyclone dust collector is provided with a second dipleg for storing fine semicoke, and the second dipleg is connected with the semicoke inlet.
In some embodiments, the gas cooling unit is provided with a primary gas cooler and a secondary gas cooler connected to each other;
the primary gas cooler is connected with the cyclone dust removal unit;
the secondary gas cooler is connected with the gas scrubbing unit.
In some embodiments, the gas scrubbing unit is provided with a gas scrubbing tower;
the top end of the gas washing tower is provided with a gas outlet and a washing water inlet;
the bottom of gas washing tower is equipped with water mortar outlet, the mortar of water mortar outlet passes through the force (forcing) pump and carries extremely the gasification feed inlet.
In some embodiments, the system further comprises a gas-solid separator, wherein the gas-solid separator is respectively connected with the bottom end of the descending gasification bed and the bottom end of the ascending dry distillation bed.
In some embodiments, the dry distillation feed inlet is provided with a pressurized feed coal lock structure.
The utility model has the advantages as follows:
the utility model discloses a gasification bed down, go upward the dry distillation bed, whirlwind dust removal unit, coal gas cooling unit and coal gas washing unit, a structure is simple, and reasonable design can adopt the fine particle coal to be the raw materials, through going upward the combination of dry distillation bed and gasification bed down, coal is by the step-by-step conversion, earlier retrieve through going upward the dry distillation bed volatile in the coal, can obtain certain coal tar and dry distillation gas, the gained coal tar of dry distillation gets into gasification bed down, move the high temperature gasification in the fluidized bed and generate coal gas down, retrieve the tar in the coal gas, behind the methane, all the other CO and H 2 As the synthesis raw material gas, the method can convert and recover the effective components in the coal to the maximum extent; it is suitable for annual light coal, and has low requirements for water content, ash content and composition of coal, and good conversion effect.
Drawings
FIG. 1 is a schematic structural view of some embodiments of the present application;
FIG. 2 is a schematic illustration of the configuration of a downer gasification bed in some embodiments of the present application;
description of reference numerals: the device comprises a downward gasification bed 1, a gasification gas inlet 11, a gasification feed inlet 12, a gasification agent inlet 13, a semicoke inlet 14, an upward carbonization bed 2, a carbonization feed inlet 21, a pressurized feeding coal lock structure 211, a cyclone dust removal unit 3, a primary cyclone dust remover 31, a first dipleg 311, a secondary cyclone dust remover 32, a second dipleg 321, a coal gas cooling unit 4, a primary coal gas cooler 41, a secondary coal gas cooler 42, a coal gas washing unit 5, a coal gas washing tower 51, a coal gas outlet 511, a washing water inlet 512, a water ash slurry outlet 513, a combustor 6 and a gas-solid separator 7.
Detailed Description
The technical solutions of the present invention will be described more clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", "front", "rear", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be mechanically coupled, may be directly coupled, or may be indirectly coupled through an intermediary. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in fig. 1 to 2, the coal conversion apparatus according to the present embodiment includes a downward gasification bed 1, an upward carbonization bed 2, a cyclone dust removal unit 3, a coal gas cooling unit 4, and a coal gas washing unit 5;
the top end of the descending gasification bed 1 is provided with a gasification gas inlet 11 and a gasification feed inlet 12, the gasification feed inlet 12 is respectively connected with the cyclone dust removal unit 3 and the coal gas washing unit 5, and the bottom end of the descending gasification bed 1 is connected with the bottom end of the ascending dry distillation bed 2;
the bottom end of the ascending dry distillation bed 2 is provided with a dry distillation feed inlet 21, and the top end of the ascending dry distillation bed 2 is connected with the cyclone dust removal unit 3;
the coal gas cooling unit 4 is respectively connected with the cyclone dust removal unit 3 and the coal gas washing unit 5.
The implementation structure is simple, the design is reasonable, and the fine-particle coal can be adopted as the raw material to pass through the ascending dry distillation bed 2 and the descending gasificationThe combination of the bed 1, the coal is converted step by step, the volatile component in the coal is recovered through the ascending dry distillation bed 2, a certain amount of coal tar and dry distillation gas can be obtained, the coal tar obtained by dry distillation enters the descending gasification bed 1, the coal tar is gasified at high temperature in the descending gasification bed 1 to generate coal gas, and after the tar and methane in the coal gas are recovered, the rest CO and H 2 As the synthesis raw material gas, the active ingredients in the coal can be converted and recovered to the maximum extent; it is suitable for annual light coal, and has low requirements for water content, ash content and composition of coal, and good conversion effect.
Specifically, the downer gasification bed 1 is set as a downer spouted bed; the ascending dry distillation bed 2 is arranged as an ascending conveying bed.
In this embodiment, the downward gasification bed 1 is set as a downward spouted bed, which facilitates the dispersion of the raw materials by spouting, so as to perform better gasification, and the upward carbonization bed 2 is set as an upward conveying bed, so that the raw materials can be entrained and conveyed by high-temperature gas, which facilitates the conveyance and has a good carbonization effect.
Specifically, a gasification agent inlet 13 and a semicoke inlet 14 are arranged at the middle lower end of the downward gasification bed 1, and the semicoke inlet 14 is connected with the cyclone dust removal unit 3.
In the embodiment, the combustion-supporting gas may be oxygen, the semicoke inlet 14 is mainly used for adding coarse semicoke or fine semicoke separated from the cyclone dust removal unit 3, and the combustor 6 may be arranged at the position to improve the gas temperature in the furnace body through combustion, so as to facilitate gasification reaction of the semicoke.
In some embodiments, the primary cyclone 31 is provided with a first dipleg 311 for storing coarse semicoke, and the first dipleg 311 is respectively connected with the gasification feed port 12 and the semicoke inlet 14;
the secondary cyclone dust collector 32 is provided with a second dipleg 321 for storing fine semicoke, and the second dipleg 321 is connected with the semicoke inlet 14.
In this embodiment, by arranging the primary cyclone dust collector 31 and the secondary cyclone dust collector 32, the semicoke generated by dry distillation in the upward carbonization bed 2 can be separated step by step, wherein the coarse semicoke with larger particles is separated by the primary cyclone dust collector 31, most of the coarse semicoke is fed to the top end of the downward gasification bed 1, and a small part of the coarse semicoke is fed to the middle lower part of the downward gasification bed 1 for further gasification treatment; the fine semicoke with smaller particles is separated by the secondary cyclone 32 and conveyed to the middle lower part of the downer gasification bed 1 for further treatment.
In some embodiments, the gas cooling unit 4 is provided with a primary gas cooler 41 and a secondary gas cooler 42 connected to each other;
the primary gas cooler 41 is connected with the cyclone dust removal unit 3;
the secondary gas cooler 42 is connected to the gas scrubbing unit 5.
In this embodiment, the oil-type organic matters in the gas are gradually condensed by the first-stage gas cooler 41 and the second-stage gas cooler 42 for classification and recovery processing.
In some embodiments, the gas scrubbing unit 5 is provided with a gas scrubbing tower 51;
the top end of the gas washing tower 51 is provided with a gas outlet 511 and a washing water inlet;
the bottom end of the gas washing tower 51 is provided with a water cement slurry outlet 513, and the cement slurry of the water cement slurry outlet 513 is conveyed to the gasification feed port 12 by a pressurizing pump.
In the embodiment, the washing water is arranged to wash and purify the coal gas, and the coal gas purifier is simple in structure and good in purification effect.
In some embodiments, the gas-solid separator 7 is further included, and the gas-solid separator 7 is respectively connected with the bottom end of the descending gasification bed 1 and the bottom end of the ascending dry distillation bed 2.
In this embodiment, the gas-solid separator 7 is provided to facilitate separation of solids from the gasified high-temperature gas in the downward gasification bed 1, and then the high-temperature gas is sent to the upward carbonization bed 2 to perform carbonization treatment of coal.
In some embodiments, the dry distillation feed port 21 is provided with a pressurized feed coal lock 211. In this embodiment, the feeding coal lock structure 211 is provided to facilitate the feeding of the fine coal in the upward carbonization bed 2.
When the coal conversion device is used for coal conversion, coal is prepared into fine particles, the fine particles are added to the bottom of the ascending carbonization bed 2 through a pressurized coal lock, are in contact with hot gas from the descending gasification bed 1 and flow upwards by being entrained by the hot gas, the coal is heated and heated in the process, firstly, moisture in the coal is evaporated, then, volatile components in the coal are volatilized from solids in a gaseous state, after the carbonization and drying process is finished, semi-coke is generated, when the gas and the semi-coke reach the top end of the ascending carbonization bed 2, the gas and the semi-coke enter the cyclone dust removal unit 3, the semi-coke in the coal gas is separated, the separated semi-coke enters the dipleg and flows downwards along the dipleg, most of the semi-coke is led out and conveyed to the top of the descending gasification bed 1, and is added and dispersed into a hearth of the descending gasification bed 1 from the top of the descending gasification bed 1, and oxygen is also added from the top of the descending gasification bed 1 at the same time.
Firstly, oxygen and semicoke are subjected to combustion reaction to generate carbon dioxide, heat is released to heat solid particles and gas, and the semicoke combustion reaction is mainly in the form of incomplete combustion reaction along with further increase of the temperature of a hearth, and the reaction is mainly used for generating carbon monoxide; after the oxygen is consumed, carrying out reduction reaction on the semicoke and carbon dioxide to generate carbon monoxide; the reduction reaction absorbs heat, the gas temperature is reduced until the gasification reaction speed becomes slow, and in the oxidation reaction process, the moisture in the newly added fine pulverized coal and the moisture in the coal slurry are changed into water vapor which also serves as gasification reactants and reacts with the semicoke to generate hydrogen, carbon monoxide, carbon dioxide and the like.
In the upper combustion stage of the lower fluidized bed 1, the combustion temperature of the semicoke and oxygen is high, ash components are molten, molten particles are gathered to form larger slag drops, and the slag drops are cooled and solidified by gas with gradually reduced temperature in the descending process; and when the solid slag reaches the bottom of the gasification side, most of the semicoke is converted into carbon dioxide and carbon monoxide as gases and part of hydrogen, the solidified ash particles are larger, the density is higher, the solid enters a gas-solid separator 7 along with the gases, the solid slag with large particles is separated out, and finally the solid slag is discharged out of the system in a coarse ash form through pressure reduction.
The coal gas with the separated coarse ash enters the bottom of the ascending carbonization bed 2 and contacts with the added fine coal to ensure that the coal is carbonized and the temperature of the coal gas is reduced.
And the coal gas leaving the cyclone dust removal unit 3 enters a coal gas cooling unit 4, is cooled to obtain condensate, then enters a coal gas washing unit 5 for further washing and purification, the dust collected by the coal gas washing unit 5 is in the form of mortar, the mortar is conveyed to the bottom end of the gasification bed 1 through a pressurizing pump, organic matters in the dust are further converted, and the coal gas leaving the coal gas washing unit 5 is subjected to downstream further purification treatment.
Part of the semicoke from the dipleg of the cyclone dust removal unit 3 is introduced into the middle part and the lower part of the downward gasification bed 1, the semicoke is combusted by the combustor 6 and part of oxygen is added, and high-temperature flue gas generated by combustion is mixed into the gas of the downward gasification bed 1 to improve the temperature of the gas in the furnace, thereby being beneficial to the further gasification reaction of the semicoke.
High-temperature gas in the descending gasification bed 1 enters the ascending dry distillation bed 2, fine coal added into the ascending dry distillation bed 2 is subjected to dry distillation at a high temperature, condensate condensed by the coal gas condensation unit is oil organic matters, mainly comprises components of medium-temperature fractions and light fractions, is less in heavy components, is discharged out of the system after being filtered and dedusted, and is processed and recovered at the rear end.
Specifically, according to the coal conversion device provided by the application, the coal can be brown coal, long flame coal, weakly caking coal and the like. The raw coal has wide applicable range of moisture content, ash content and ash composition, the moisture content of the coal with high moisture content (such as 25-40%) in the coal can be reduced to be below 20-25% through preliminary drying, the coal ash content can reach 30% or higher, and the coal ash melting point has no obvious influence on gasification operation within the range of 1100-1500 ℃.
When the raw material coal is prepared, the coal granularity control is needed, and for coal with low moisture, the coal can be directly divided into two parts of fine coal and coal powder according to the granularity in the crushing process, the granularity is divided into about 50 micrometers, and the adjustment can be made according to specific situations. For coal with high water content, a drying unit is required to be added to remove part of water in the coal. And adding the fine coal into the ascending carbonization bed 2 through a coal lock system, and preparing the fine coal into water-coal-slurry to be delivered to the descending gasification bed 1. The operation pressure of the converter can be carried out in a wide range, and the oxidant is pure oxygen from normal pressure to high pressure (such as 8 MPa) when synthesis raw material gas (mainly H2 and CO) is generated; when industrial fuel gas is generated, air can be used as a gasifying agent and is sent into the descending gasifying bed 1; oxygen-rich gasification can also meet specific needs if necessary.
The coal conversion device comprises a downward gasification side spray bed and an upward carbonization side conveying bed, fine particles in coal are added to the lower part of the carbonization side conveying bed through a pressurized coal lock, the coal is contacted with hot gas (900-1100 ℃) from the bottom of a gasification side and flows upwards by being entrained by the gas, the conveying bed adopts a high upward speed, the gas can reach 15m/s, the coal is heated and heated in the process, the moisture in the coal is evaporated firstly, then the volatile components in the coal are volatilized from solids in a gaseous state, semicoke is generated after the carbonization drying process is finished, when the gas and the semicoke reach the top end of the carbonization side together, (the temperature is 300-600 ℃), the gas enters a primary cyclone dust collector 31 to separate the coarse particles from the gas, the gas leaving the primary cyclone dust collector 31 enters a secondary cyclone dust collector 32 again, the fine particles in the gas are further separated, the coarse particles are coarse semicoke, the fine particles are fine semicoke, most of the coarse particles are conveyed into the top of the downward gasification bed 1, the slag and the slag is melted with high combustion temperature (1600-1600 ℃, and the slag is gradually melted and the slag is cooled to form larger ash drops.
And when the solid slag reaches the bottom of the gasification side, most of the semicoke is converted into carbon dioxide and carbon monoxide as gases and part of hydrogen, the solidified ash particles are larger, the density is higher, the solid enters a gas-solid separator 7 along with the gases, the solid slag with large particles is separated out, and finally the solid slag is discharged out of the system in a coarse ash form through pressure reduction.
The coal gas leaving the primary cyclone dust collector 31 enters a primary coal gas cooler 41, is cooled to 250 ℃ by temperature control to obtain condensate A, then enters a secondary coal gas cooler 42, is cooled to 150 ℃ by temperature control to obtain condensate B, and then enters a washing tower for further washing and purification. The dust collected by the washing tower is sent to a gasification side high-temperature area of the converter in the form of mortar by a pressure pump, so that organic matters in the dust are further converted. The coal gas leaving the washing tower goes to the downstream for further purification treatment.
The method can adopt annual light coal with high water content and high ash content, and the change of the coal quality has less influence on the operation of the converter. Condensate generated in the conversion process is coal tar-like substances, most of the condensate is medium light oil, the heavy oil is less, and the oil is used as a byproduct, so that the utilization value of coal can be maximally improved.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the concept of the present invention, several variations and modifications can be made, which all fall within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (10)
1. A coal conversion device is characterized by comprising a descending gasification bed, an ascending dry distillation bed, a cyclone dust removal unit, a coal gas cooling unit and a coal gas washing unit;
the top end of the descending gasification bed is provided with a gasification gas inlet and a gasification feed inlet, the gasification feed inlet is respectively connected with the cyclone dust removal unit and the coal gas washing unit, and the bottom end of the descending gasification bed is connected with the bottom end of the ascending dry distillation bed;
the bottom end of the ascending dry distillation bed is provided with a dry distillation feed inlet, and the top end of the ascending dry distillation bed is connected with the cyclone dust removal unit;
the coal gas cooling unit is respectively connected with the cyclone dust removal unit and the coal gas washing unit.
2. The coal conversion plant according to claim 1, wherein the downer gasification bed is arranged as a downer spouted bed; the ascending carbonization bed is arranged as an ascending conveying bed.
3. The coal conversion plant according to claim 1, wherein the middle lower end of the downer gasification bed is provided with a gasification agent inlet and a semicoke inlet, and the semicoke inlet is connected with the cyclone dust removal unit.
4. The coal conversion plant of claim 3, further comprising a burner, said gasification agent inlet and said char inlet being connected to said burner, respectively.
5. The coal conversion plant according to claim 3, wherein the cyclone dust removal unit is provided with a primary cyclone dust collector and a secondary cyclone dust collector which are connected with each other;
the primary cyclone dust collector is respectively connected with the top end of the ascending dry distillation bed, the gasification feed inlet and the semicoke inlet;
and the secondary cyclone dust collector is respectively connected with the coal gas cooling unit and the semicoke inlet.
6. The coal conversion plant of claim 5, wherein the primary cyclone is provided with a first dipleg for storing coarse char, the first dipleg being connected to the gasification feed inlet and the char inlet, respectively;
and the secondary cyclone dust collector is provided with a second dipleg for storing fine semicoke, and the second dipleg is connected with the semicoke inlet.
7. The coal conversion plant according to claim 1, wherein the gas cooling unit is provided with a primary gas cooler and a secondary gas cooler connected to each other;
the primary gas cooler is connected with the cyclone dust removal unit;
the secondary gas cooler is connected with the gas scrubbing unit.
8. The coal conversion plant of claim 1, wherein the gas scrubbing unit is provided with a gas scrubbing tower;
the top end of the gas washing tower is provided with a gas outlet and a washing water inlet;
the bottom of gas washing tower is equipped with water mortar outlet, the mortar of water mortar outlet passes through the force (forcing) pump and carries extremely the gasification feed inlet.
9. The coal conversion plant of claim 1, further comprising a gas-solid separator connected to the bottom end of the downer gasification bed and the bottom end of the upgoing destructive distillation bed, respectively.
10. The coal conversion plant according to claim 1, wherein the dry distillation feed inlet is provided with a pressure feed coal lock arrangement.
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| CN202222112832.5U CN217733013U (en) | 2022-08-11 | 2022-08-11 | Coal conversion device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115322813A (en) * | 2022-08-11 | 2022-11-11 | 李冶 | Integrated coal conversion device and conversion method thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115322813A (en) * | 2022-08-11 | 2022-11-11 | 李冶 | Integrated coal conversion device and conversion method thereof |
| CN115322813B (en) * | 2022-08-11 | 2023-11-28 | 李冶 | Integrated coal conversion device and conversion method thereof |
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