CN219279815U - Continuous slag discharging system for gasification device - Google Patents
Continuous slag discharging system for gasification device Download PDFInfo
- Publication number
- CN219279815U CN219279815U CN202320380577.4U CN202320380577U CN219279815U CN 219279815 U CN219279815 U CN 219279815U CN 202320380577 U CN202320380577 U CN 202320380577U CN 219279815 U CN219279815 U CN 219279815U
- Authority
- CN
- China
- Prior art keywords
- slag
- pressure reducing
- buffer chamber
- solid
- liquid separation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002893 slag Substances 0.000 title claims abstract description 178
- 238000002309 gasification Methods 0.000 title claims abstract description 46
- 238000007599 discharging Methods 0.000 title claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 238000000926 separation method Methods 0.000 claims abstract description 40
- 239000012530 fluid Substances 0.000 claims abstract description 28
- 239000007787 solid Substances 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 62
- 239000010797 grey water Substances 0.000 claims description 46
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 239000010866 blackwater Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 2
- 239000003638 chemical reducing agent Substances 0.000 abstract description 28
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 32
- 238000000034 method Methods 0.000 description 15
- 238000010586 diagram Methods 0.000 description 10
- 238000010791 quenching Methods 0.000 description 8
- 239000003245 coal Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 238000000151 deposition Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Images
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The utility model provides a continuous slag discharging system for a gasification device. The continuous slag discharging system comprises a buffer chamber, at least one pressure reducing device and a solid-liquid separation device which are connected in sequence; the buffer chamber comprises a feed inlet, a first fluid inlet and a discharge outlet; the feed inlet of the buffer chamber is connected with the outlet of the slag breaker; the buffer chamber is used for providing a space for mixing the slag crushed by the slag crusher with the first fluid fed by the first fluid inlet; the discharge port of the buffer chamber is connected with the inlet of each pressure reducing device to realize the input of slag into the pressure reducing devices through the first fluid introduced into the buffer chamber. The continuous slag discharging system can realize continuous slag discharging, has higher safety, can reduce the frame height of the system, reduce investment and improve reliability; and through the design of the pressure reducer with better wear resistance, the blockage of solid slag in the pipeline can be prevented, and the service life of the device can be prolonged.
Description
Technical Field
The utility model relates to a continuous slag discharging system for a gasification device.
Background
The coal gasification process is a process of converting the combustible part of coal or char into synthesis gas/combustible gas by chemical reaction with oxygen (air, oxygen-enriched or industrially pure oxygen) and steam as gasifying agents. Entrained flow gasification technology is the main stream technology of coal gasification at present because of the characteristics of good technical indexes, high treatment load, good environment and the like. The entrained flow gasification process is characterized by high temperature, namely, partial oxidation reaction is carried out between pure oxygen/oxidant and coal, so that most combustible matters in the coal are synthesized into gas/combustible gas; coal ash (mainly oxides, inorganic salts and the like) flows out of the gasification chamber in the form of liquid slag at high temperature and enters a chilling chamber or a slag basin. The cooled slag is deposited at the bottom of the chilling chamber or the slag sedimentation tank in the form of glass or solid slag, and is discharged out of the gasifier in a pressure alternating mode through a lock hopper.
In the existing lock bucket pressure alternating slag discharging device, a large amount of space (about 25 m) is occupied due to arrangement of devices such as a lock bucket and a cut-off valve, so that a gasification frame is very high, the lock bucket is used for collecting slag in industry, after the slag is collected fully or in a certain amount, an inlet valve is closed, pressure is released, an outlet valve is opened, and slag discharging is realized.
Disclosure of Invention
The continuous slag discharging system for the gasification device is provided for overcoming the defects that the gasification frame is high, the slag discharging process is easy to block and continuous slag discharging cannot be realized in the prior art. The continuous slag discharging system can realize continuous slag discharging, has higher safety, can reduce the frame height of the system, reduce investment and improve reliability; and through the design of the pressure reducer with better wear resistance, the blockage of solid slag in the pipeline can be prevented, and the service life of the device can be prolonged.
The utility model solves the technical problems by the following technical scheme:
the utility model provides a continuous slag discharging system for a gasification device, which comprises a gasification furnace, a chilling chamber and a slag breaker which are connected up and down, wherein the continuous slag discharging system comprises a buffer chamber, at least one pressure reducing device and a solid-liquid separation device which are connected in sequence; wherein,,
the buffer chamber comprises a feed inlet, a first fluid inlet and a discharge outlet; the feed inlet of the buffer chamber is connected with the outlet of the slag breaker; the buffer chamber is used for providing a space for mixing slag materials crushed by the slag crusher with the first fluid fed by the first fluid inlet;
the discharge port of the buffer chamber is connected with the inlet of each pressure reducing device so as to realize that the slag is input into the pressure reducing devices through the first fluid introduced into the buffer chamber;
the solid-liquid separation device is used for carrying out solid-liquid separation on the slag water discharged by the pressure reducing device;
the slag breaker is used for breaking slag generated by the gasifier and then discharging the broken slag into the buffer chamber.
In the utility model, preferably, a chilled water inlet pipeline and a black water outlet pipeline are arranged at the top of the chilling chamber and are used for cooling and settling the slag in the gasifier.
In the present utility model, preferably, in the gasification device, the gasification furnace, the quench chamber and the slag breaker are integrally formed from top to bottom.
In the present utility model, preferably, the buffer chamber is integrally formed below the slag breaker.
In the present utility model, preferably, the buffer chamber is independently disposed below the slag breaker.
In the utility model, the buffer chamber is a small space no matter the buffer chamber is integrally formed with the slag breaker or independently arranged, and the buffer chamber is used for temporarily storing solid materials and arranging a continuous pressure reducer.
In the present utility model, the pressure reducing means is preferably provided on the outer side surface or below the bottom of the buffer chamber.
In the present utility model, preferably, the pressure reducing means includes one or more of a tesla valve, a multi-stage orifice plate, and a pressure reducing orifice plate.
In the present utility model, preferably, a pipeline connecting the pressure reducing device and the solid-liquid separation device is provided with a plurality of shut-off valves for switching and isolating; on the one hand, the number of openings can be determined according to the pressure drop of the pressure reducing device; and on the other hand, the device is used for switching the pressurizer.
In the present utility model, preferably, a pressurizing pipeline with a pressurizer is provided on a pipeline connecting the pressure reducing device and the solid-liquid separation device, for adjusting the pressure of the slag water in the outlet pipeline of the pressure reducing device. On the one hand, the protection and slag deposition resistance can be carried out when the pressure reducing device is not in use; on the other hand, the back flushing can be carried out after the pressurizer is blocked.
The pressurizer can be a high-pressure ash water pump or a high-temperature ash water pump of a coal gasification device which is conventional in the art, and can also be a separate high-pressure water pump for providing high-pressure ash water.
Preferably, the pressurizing pipeline is arranged at the upstream of the shut-off valve, and the upstream is measured along the flow direction of the slag water and is positioned at the front part of the outlet pipeline of the pressure reducing device.
In the present utility model, preferably, the number of the pressure reducing devices is 1 to 10; more preferably, when the number of the pressure reducing devices is greater than 1, the inlets of the pressure reducing devices are respectively connected with the first fluid outlets of the buffer chambers, so that the pressure reducing devices are connected in parallel. The parallel connection mode can reduce the pressure and control the outflow of slag flow, thereby realizing the increase of the treatment capacity of slag discharge and the increase of the reliability of slag discharge, for example, when 3 pressure reducers are in parallel operation, when 1 pressure reducer is blocked, the load of the other 2 pressure reducers can be properly increased, and the blockage can be cleared. And when the buffer chamber is connected in series with each of the pressure reducers in turn, the pressure is reduced from 6.5MpaG to 0.1MpaG.
In the utility model, preferably, the solid-liquid separation device is a traditional slag dragging machine or a novel slag dragging machine and is used for carrying out sedimentation separation on slag water from the decompression device in the slag chamber.
Preferably, the slag scooping machine is arranged below or beside the gasification device.
Wherein, preferably, the slag scooping machine is arranged below or beside the pressure reducing device.
Preferably, the difference between the height of the slag water inlet of the slag dragging machine and the height of the outlet of the pressure reducing device is 0.1-10 m.
Wherein, preferably, the distance between the slag water inlet of the slag dragging machine and the outlet height of the pressurizing pipeline is 2m.
In the present utility model, preferably, the solid-liquid separation device includes an ash chamber and an ash water chamber separated by a baffle plate having an overflow port; more preferably, the overflow port is arranged in the middle of the baffle plate and is used for enabling supernatant liquid in the ash chamber to flow into the ash chamber.
In the present utility model, preferably, the outlet of the solid-liquid separation device is provided with a slag pool circulating pump.
In the present utility model, preferably, the continuous slag discharging system further includes a grey water treatment unit, the grey water treatment unit is disposed at a downstream of the solid-liquid separation device, and the downstream is a portion after the material in the flow direction; and is the following structure (1) or structure (2):
the structure (1) comprises a grey water treatment unit, wherein a tube side inlet of the grey water treatment unit is connected with a grey water outlet of the solid-liquid separation device, and a tube side outlet of the grey water treatment unit is connected with a first fluid inlet of the buffer chamber;
the ash water treatment unit comprises a vacuum flash tank, a clarifying tank and an ash water tank which are sequentially connected; the vacuum flash tank is connected with a gray water outlet of the solid-liquid separation device, and the gray water tank is connected with a first fluid inlet of the buffer chamber; preferably, a high-pressure water pump is arranged on a pipeline connecting the ash water tank and the buffer chamber.
In the present utility model, preferably, the continuous slag discharging method using the continuous slag discharging system as described above comprises the following steps:
s1, collecting slag of the gasification device in the buffer chamber;
s2, introducing a first fluid into the buffer chamber, enabling the formed suspension to pass through at least one pressure reducing device, performing solid-liquid separation to obtain ash water and ash, and discharging the ash.
In S1, preferably, the method for collecting the slag includes quenching the slag of the gasifier and depositing the slag at the bottom of the quench chamber.
In S1, preferably, the D50 particle size of the slag crushed by the slag crusher is 0.1-5 cm; more preferably 0.2cm or 1cm.
In S1, the maximum grain size of the slag crushed by the slag crusher is preferably 5cm.
In S1, the size of the slag crushed by the slag crusher is preferably millimeter.
Wherein, the high-performance slag breaker capable of breaking slag into millimeter level and the pressure reducing device with anti-blocking and high pressure difference can realize the smooth discharge of solid slag.
In S2, the first fluid is preferably mixed with the slag to form the slag water. The buffer section is internally provided with flushing stirring water, so that particles are vigorously turbulent and suspended in the buffer tank.
In S2, preferably, the first fluid is high-pressure grey water, and the pressure of the high-pressure grey water is greater than the pressure of the buffer chamber.
In S2, the target pressure of the pressure reducing device is preferably 0 to 0.2MPa.
In S2, the temperature of the suspension after passing through the pressure reducing device is preferably 50 to 90 ℃, more preferably 70 ℃.
In S2, the solid content of the slag water in the pressure reducing device is preferably 0.1 to 60%, more preferably 5%.
In S2, preferably, the slag water is pressurized by a pressurizer before entering the solid-liquid separation device; more preferably, the outlet pressure of the pressurizing pipe connected to the pressurizer is 2kPa.
In S2, preferably, the temperature of the ash water after the solid-liquid separation is 80 ℃;
in the present utility model, preferably, the continuous slag discharging method further includes step S3: the grey water in the step S2 is subjected to heat exchange and then flows back to the buffer chamber; or removing the solids in the grey water in the step S2, and pressurizing and refluxing the grey water to the buffer chamber.
Preferably, the method for removing the solids in the grey water sequentially comprises the following steps: flash evaporation and sedimentation.
Preferably, when the gasification furnace, the chilling chamber, the slag breaker and the buffer chamber are of an integrated structure, the pressure of the ash water pressurized and returned to the buffer chamber is higher than the pressure of the gasification furnace; more preferably, the pressure of the ash water pressurized and returned to the buffer chamber is 0.5MPa higher than the pressure of the gasification furnace; for example, when the pressure of the gasification furnace is 4.0MPa, the pressure of the pressurized return ash water to the buffer chamber is 4.5MPa; for example, when the pressure of the gasification furnace is 6.5MPa, the pressure of the pressurized return ash water to the buffer chamber is 7.0MPa.
Wherein, the temperature of the heat exchange is preferably 40-60 ℃, more preferably 45 ℃.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the utility model.
The reagents and materials used in the present utility model are commercially available.
The utility model has the positive progress effects that:
1. the continuous slag discharging system can realize continuous slag discharging, has higher safety, can reduce the frame height of the system, reduce investment and improve reliability.
2. The pressure reducer in the continuous slag discharging system has better abrasion resistance, can prevent solid slag from being blocked in a pipeline, and can prolong the service life of the device.
Drawings
FIG. 1 is a schematic diagram of a continuous slag discharging system according to embodiment 1 of the present utility model;
FIG. 2 is a schematic diagram of a continuous slag discharging system according to embodiment 2 of the present utility model;
FIG. 3 is a schematic diagram of a Tesla valve as a pressure reducer in a preferred embodiment of the utility model;
FIG. 4 is a schematic view of a preferred embodiment of the present utility model using a multi-stage orifice plate as a pressure reducer;
FIG. 5 is a schematic view of a preferred embodiment of the present utility model with an optimized multi-stage orifice plate as a pressure reducer;
fig. 6 is a schematic diagram of a preferred embodiment of the present utility model using an optimized pressure relief orifice as a pressure reducer.
Reference numerals illustrate:
First fluid inlet 202
Pressure reducing device 3
Shut-off valve 301
Solid-liquid separation device 4
Slag pool circulating pump 403
Grey water treatment unit 5
High-pressure ash water pump 504
Detailed Description
The utility model is further illustrated by means of the following examples, which are not intended to limit the scope of the utility model. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.
Example 1
Fig. 1 is a schematic structural diagram of a continuous slag discharging system according to the present embodiment.
The embodiment is a continuous slag discharging system for a gasification device 1, the gasification device 1 comprises a gasification furnace 101, a chilling chamber 102 and a slag breaker 103 which are connected up and down and are integrally formed, a chilling water inlet pipeline and a black water outlet pipeline are arranged at the top of the chilling chamber 102 and are used for cooling and settling slag in the gasification furnace 101, and the slag breaker 103 is used for breaking slag generated by the gasification furnace 101 and then discharging the broken slag into a buffer chamber 2. The continuous slag discharging system comprises a buffer chamber 2, four pressure reducing devices 3 and a solid-liquid separation device 4 which are connected in sequence; the buffer chamber 2 comprises a feed inlet 201, a first fluid inlet 202 and a discharge outlet 203; the feed inlet 201 of the buffer chamber 2 is connected with the outlet of the slag breaker 103; the buffer chamber 2 is used for providing a space for mixing the slag crushed by the slag crusher 103 with the first fluid fed by the first fluid inlet 202; the buffer chamber 2 is integrally formed below the slag breaker 103; the discharge port 203 of the buffer chamber 2 is connected to the inlet of each pressure reducing device 3, so that the four pressure reducing devices 3 are connected in parallel.
The pressure reducing device 3 is arranged on the outer side surface of the buffer chamber 2; the pressure reducing device 3 can be a Tesla valve, a multi-stage orifice plate or a pressure reducing orifice plate. FIG. 3 is a schematic diagram of a Tesla valve as a pressure reducer; FIG. 4 is a schematic diagram of a multi-stage orifice plate as a pressure reducer; FIG. 5 is a schematic diagram of a configuration with an optimized multi-stage orifice plate as a pressure reducer; fig. 6 is a schematic diagram of a configuration with an optimized pressure relief orifice plate as a pressure reducer. A pressurizing pipeline 312 with a pressurizer 302 is arranged on a pipeline connecting the pressure reducing device 3 and the solid-liquid separation device 4 and is used for adjusting the pressure of slag water in an outlet pipeline of the pressure reducing device 3; a plurality of cut-off valves 301 are arranged on the pipeline connecting the pressure reducing device 3 and the solid-liquid separation device 4; the pressurizing line 312 is provided upstream of the shut-off valve 301; upstream is a flow direction meter along slag water, and is positioned at the front part of an outlet pipeline of the pressure reducing device 3;
the solid-liquid separation device 4 is a slag extractor which is conventional in the art. The slag dragging machine is arranged below the gasification device 1; the slag dragging machine is arranged below the pressure reducing device 3; the height difference between the slag water inlet of the slag dragging machine and the outlet of the pressure reducing device 3 is less than 0.2m; the slag conveyor is arranged below the pressurizer 302; the slag water inlet of the slag machine is 2m from the height of the outlet of the pressurized line 312.
The solid-liquid separation device 4 includes an ash chamber 401 and an ash water chamber 402 partitioned by a baffle plate having an overflow port 404; an overflow port 404 is arranged in the middle of the baffle plate and is used for enabling supernatant liquid in the ash chamber 401 to flow into the ash chamber 402; the outlet of the solid-liquid separation device 4 is provided with a slag pool circulating pump 403.
The continuous slag discharging system further comprises a grey water treatment unit 5, the grey water treatment unit 5 is arranged at the downstream of the solid-liquid separation device 4, and the grey water treatment unit 5 has the following structure:
the grey water treatment unit 5 comprises a vacuum flash tank 501, a clarifying tank 502 and a grey water tank 503 which are connected in sequence; the vacuum flash tank 501 is connected with a grey water outlet of the solid-liquid separation device 4, and the grey water tank 503 is connected with the first fluid inlet 202 of the buffer chamber 2; a high-pressure water pump 504 is arranged on the pipeline connecting the ash water tank 503 with the buffer chamber 2.
Example 2
Fig. 2 is a schematic structural diagram of the continuous slag discharging system of the present embodiment.
The continuous slag discharging system of this embodiment is the same as that of embodiment 1, except that the structure of the grey water treatment unit 5 is as follows:
the grey water treatment unit 5 comprises a grey water cooler 505, wherein a tube side inlet of the grey water cooler 505 is connected with a grey water outlet of the solid-liquid separation device 4, and a tube side outlet of the grey water cooler 505 is connected with the first fluid inlet 202 of the buffer chamber 2.
Example 3
This embodiment is a continuous slag discharging method, which adopts the continuous slag discharging system as in embodiment 1 or embodiment 2, comprising the steps of:
s1, collecting slag of a gasification device 1, and enabling solid slag obtained after crushing to enter a buffer chamber 2; the slag collecting method comprises quenching slag of the gasifier 101 and depositing the quenched slag at the bottom of the chilling chamber 102; the D50 grain diameter of the crushed slag is 0.1-5 cm;
s2, introducing high-pressure ash water into the buffer chamber 2, and mixing the high-pressure ash water with slag to form slag water; the formed suspension passes through 4 pressure reducing devices 3 with target pressure of 0-0.2 MPa, and the solid content of fluid in the pressure reducing devices 3 is 5%; before entering the solid-liquid separation device 4, the slag water is pressurized by adopting a pressurizer 302, so that the outlet pressure of a pressurizing pipeline 312 is 2kPa; then solid-liquid separation is carried out, ash water and ash residue at 80 ℃ are obtained after the solid-liquid separation, and the ash residue is discharged.
S3, the grey water can be sent to the grey water treatment unit 5 according to the traditional process flow, sequentially passes through the vacuum flash tank 501, the sedimentation tank 502 and the grey water tank 503, and finally returns to the buffer section 2 below the slag breaker 103 under the action of the high-pressure grey water pump 504 (adopting the continuous slag discharging system of the embodiment 1); alternatively, it may be pressurized to a pressure greater than that of the quench chamber 102 and passed through the grey water cooler 505 before entering the buffer zone 2 (using the continuous slag removal system of example 2).
Example 4
The continuous slag removal method of example 3 was used. The gasification apparatus 1 for end use of production chemicals, wherein the daily treatment scale of the gasification furnace 101 is 1500 tons/day, the flow of slag into the quench chamber 102 is 5 tons/hour and the pressure is 6.5MPa. The slag breaker 103 breaks the slag into a D50 particle size of 2mm and a maximum particle size of 5mm. Setting 4 slag water pressure reducers, and 2-step configuration; the circulating water quantity is 93 tons/hour, and the high-pressure grey water of the pressurizing pipeline 312 arranged behind the pressure reducing device 3 comes from an evaporation hot water tower (or high-temperature washing water) and is used for protecting the standby pressure reducers (the flow liquid level of each pressure reducer is 1 ton/hour); the flow rate of the single slag water pressure reducing device 3 is 50 tons/hour. The temperature in the buffer section was controlled to 70 c by adjusting the heat exchange amount of the grey water cooler 505. The height of the slag dragging machine from the slag water reducing valve is 1m.
Industrial operation shows that the pressure after the pressure reducer is indicated as 0.01MPa (G), the pressure reducer is free from blockage, and the local maximum thinning of the pressure reducer is about 0.1mm after 60 days of operation. The frame of the gasification unit is about 25m lower than the traditional process frame.
Example 5
The continuous slag removal method of example 3 was used. The gasification apparatus 1 for end use of production chemicals, wherein the daily treatment scale of the gasification furnace 101 is 3000 tons/day, the flow rate of slag into the quench chamber 102 is 10 tons/hour, and the pressure is 6.5MPa. The slag breaker 103 breaks the slag into a D50 particle size of 1cm and a maximum particle size of 5cm. Setting 6 slag water pressure reducers, and 3-opening 3-standby configuration; the circulating water quantity is 180 tons/hour, and the high-pressure grey water of the pressurizing pipeline 312 arranged behind the pressure reducing device 3 comes from an evaporation hot water tower (or high-temperature washing water) and is used for protecting the standby pressure reducers (the flow liquid level of each pressure reducer is 2 tons/hour); the flow rate of the single slag water pressure reducing device 3 was 61 tons/hour. The temperature in the buffer section was controlled to 70 c by adjusting the heat exchange amount of the grey water cooler 505. The height of the slag dragging machine from the slag water reducing valve is 1m.
Industrial operation shows that the pressure after the pressure reducer is indicated as 0.01MPa (G), the pressure reducer is free from blockage, and the local maximum thinning of the pressure reducer is about 0.1mm after 60 days of operation. The gasification frame of the gasification device is about 35m lower than the traditional process frame.
Claims (10)
1. The continuous slag discharging system is used for a gasification device, and the gasification device comprises a gasification furnace, a chilling chamber and a slag breaker which are connected up and down, and is characterized by comprising a buffer chamber, at least one decompression device and a solid-liquid separation device which are connected in sequence; wherein,,
the buffer chamber comprises a feed inlet, a first fluid inlet and a discharge outlet; the feed inlet of the buffer chamber is connected with the outlet of the slag breaker; the buffer chamber is used for providing a space for mixing slag materials crushed by the slag crusher with the first fluid fed by the first fluid inlet;
the discharge port of the buffer chamber is connected with the inlet of each pressure reducing device so as to realize that the slag is input into the pressure reducing devices through the first fluid introduced into the buffer chamber;
the solid-liquid separation device is used for carrying out solid-liquid separation on the slag water discharged by the pressure reducing device;
the slag breaker is used for breaking slag generated by the gasifier and then discharging the broken slag into the buffer chamber.
2. The continuous slag removal system of claim 1, wherein a chilled water inlet pipeline and a black water outlet pipeline are arranged at the top of the chilling chamber and are used for cooling and settling the slag in the gasifier;
in the gasification device, the gasification furnace, the chilling chamber and the slag breaker are integrally formed from top to bottom.
3. The continuous slag discharging system as set forth in claim 1, wherein said buffer chamber is integrally formed below said slag breaker;
or the buffer chamber is independently arranged below the slag breaker.
4. The continuous slag removal system of claim 1, wherein the pressure relief device meets one or more of the following conditions:
a. the pressure reducing device is arranged on the outer side surface or below the bottom of the buffer chamber;
b. the pressure reducing device comprises one or more of a tesla valve, a multi-stage orifice plate and a pressure reducing orifice plate;
c. a plurality of cut-off valves are arranged on a pipeline connecting the pressure reducing device and the solid-liquid separation device;
d. a pressurizing pipeline with a pressurizer is arranged on a pipeline connecting the pressure reducing device and the solid-liquid separation device and is used for adjusting the pressure of slag water in an outlet pipeline of the pressure reducing device;
e. the number of the pressure reducing devices is 1-10; when the number of the pressure reducing devices is greater than 1, the inlets of the pressure reducing devices are respectively connected with the discharge holes of the buffer chambers, so that the pressure reducing devices are connected in parallel;
or, the solid-liquid separation device is a slag dragging machine.
5. The continuous slag removal system of claim 4, wherein said pressurized line is disposed upstream of said shut-off valve;
the slag dragging machine is arranged below or beside the gasification device;
the slag dragging machine is arranged below or beside the pressure reducing device.
6. The continuous slag discharging system as claimed in claim 5, wherein the difference in height between the slag water inlet of the slag extractor and the outlet of the pressure reducing device is 0.1-10 m;
or the distance between the slag water inlet of the slag dragging machine and the outlet height of the pressurizing pipeline is 2m.
7. The continuous slag removal system of claim 1, wherein the solid liquid separation device comprises an ash chamber and a grey water chamber separated by a baffle comprising an overflow port;
and the outlet of the solid-liquid separation device is provided with a slag pool circulating pump.
8. The continuous slag removal system of claim 7, wherein said overflow port is provided in the middle of said baffle for flowing supernatant fluid from said ash chamber into said ash chamber.
9. The continuous slag discharging system as set forth in claim 1, further comprising a grey water treatment unit provided downstream of said solid-liquid separation device and having the following structure (1) or structure (2):
the structure (1) comprises a grey water treatment unit, wherein a tube side inlet of the grey water treatment unit is connected with a grey water outlet of the solid-liquid separation device, and a tube side outlet of the grey water treatment unit is connected with a first fluid inlet of the buffer chamber;
the ash water treatment unit comprises a vacuum flash tank, a clarifying tank and an ash water tank which are sequentially connected; the vacuum flash tank is connected with a grey water outlet of the solid-liquid separation device, and the grey water tank is connected with a first fluid inlet of the buffer chamber.
10. The continuous slag discharging system of claim 9, wherein a high pressure water pump is provided on a pipe connecting said ash chute and said buffer chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320380577.4U CN219279815U (en) | 2023-03-02 | 2023-03-02 | Continuous slag discharging system for gasification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320380577.4U CN219279815U (en) | 2023-03-02 | 2023-03-02 | Continuous slag discharging system for gasification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219279815U true CN219279815U (en) | 2023-06-30 |
Family
ID=86911857
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320380577.4U Active CN219279815U (en) | 2023-03-02 | 2023-03-02 | Continuous slag discharging system for gasification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219279815U (en) |
-
2023
- 2023-03-02 CN CN202320380577.4U patent/CN219279815U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2009270461B2 (en) | Device for the removal of clinker from a coal gasification reactor | |
| US4381924A (en) | Process for sluicing residues from the pressure system of a pressure gasification tank | |
| CN102021035A (en) | System for preparing solid, liquid and gas products from coal and biomass and method using same | |
| CN106398743B (en) | A kind of petroleum coke conveys dewatering system | |
| CN103031156A (en) | Dry-process slag discharge device and method for entrained flow bed | |
| CN103517965A (en) | Closed coke slurry system and method for gaining sellable petroleum coke pieces out of solidified petroleum coke in a coke drum unit | |
| CN109161618A (en) | A kind of blast-furnace slag processing system and treatment process | |
| CN219279815U (en) | Continuous slag discharging system for gasification device | |
| CN109575996B (en) | Method for preparing synthesis gas by co-gasification of coal and heavy oil | |
| CN209906854U (en) | System for retrieve metal in follow hydrometallurgy zinc-copper sediment | |
| CN101942343A (en) | Pressurized-gasification solid-state wet-type deslagging device for carbonaceous organic material and method | |
| CN203972022U (en) | A kind of gasification furnace major path slag crusher | |
| WO2006005653A1 (en) | Process and apparatus for granulating a melt | |
| CN106623366A (en) | System for treating high-concentration refractory organic hazardous waste WF through homogenate fluid SCWO | |
| CN102746086B (en) | Technique and device for coproducing carbide slag cement in a dry-method acetylene process | |
| CN109072100B (en) | Slag discharge system, gasification furnace, and slag filtration method | |
| CN209668959U (en) | A kind of water coke coal slurry gasification production Heisui River recovery system | |
| CN217202611U (en) | Coal gasification deslagging system and slag conveyor assembly thereof | |
| CN110734790A (en) | dry-method pressure-reducing ash-discharging device and method | |
| CN206063961U (en) | A kind of gasification furnace usage on black water recovery system | |
| CN114832497B (en) | Carbide slag hydrocyclone impurity removal system | |
| CN104084262A (en) | Gasifier large-channel slag crusher | |
| CN113387501B (en) | Solid-black-containing water treatment and recycling device and method | |
| CN212998576U (en) | On-line sand-discharging emptying sand-collecting container device | |
| CN113897466B (en) | Blast furnace slag flushing device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |