CN210506234U - Entrained flow bed gasification equipment - Google Patents
Entrained flow bed gasification equipment Download PDFInfo
- Publication number
- CN210506234U CN210506234U CN201921511653.0U CN201921511653U CN210506234U CN 210506234 U CN210506234 U CN 210506234U CN 201921511653 U CN201921511653 U CN 201921511653U CN 210506234 U CN210506234 U CN 210506234U
- Authority
- CN
- China
- Prior art keywords
- combustion chamber
- water
- pipe
- convection
- waste boiler
- 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
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Gasification And Melting Of Waste (AREA)
Abstract
By adopting the design of the radiation waste boiler and the convection waste boiler, compared with the technology of only the radiation waste boiler or only the convection waste boiler, the equipment can generate more steam, the energy efficiency and the coal utilization rate can be obviously improved, the lower part of the convection waste boiler is coupled with a chilling chamber, the water-gas ratio can be adjusted according to the requirements of subsequent devices while the crude gas is cooled and dedusted, the process flow is more optimized, and the investment of subsequent equipment such as a Venturi, a carbon washing tower and the like is reduced; simultaneously, a plurality of nozzle devices of bottom region edge combustion chamber barrel of combustion chamber around evenly distributed compare with single burner device gasification technique, many nozzle devices can let buggy and oxygen form stronger torrent effect in the gasifier, and the gasifier is easily enlargied, and can not reduce carbon conversion rate, and this application provides an suitability is strong, and coal utilization ratio and efficiency are high, and the entrained flow gasification equipment that process flow is more optimized.
Description
Technical Field
The application relates to the technical field of coal gasification, in particular to entrained flow gasification equipment.
Background
The gasification reaction of coal hydrogenation is a thermochemical process, which takes pulverized coal (usually pulverized coal with the diameter less than 75 μm) as a raw material and hydrogen as a gasifying agent to react under the conditions of high temperature and high pressure to generate crude gas and light tar. Wherein, the crude gas can be subjected to operations such as separation and the like to obtain the methane-rich gas. At present, the pulverized coal hydro-gasification process mainly adopts an entrained flow bed gasification technology.
The entrained flow bed gasification technology is an important way for developing clean coal gasification technology, and is divided into two modes of dry coal powder feeding and coal water slurry feeding according to different coal conveying modes. The dry coal powder pressurized entrained flow gasification technology is the mainstream direction in the current coal gasification technology due to wide coal variety applicability, high gasification efficiency and lower specific oxygen consumption than the coal water slurry feeding; the entrained-flow bed gasification technology is divided into a waste boiler process gasification technology and a chilling process gasification technology according to different modes of treating high-temperature coal gas. The main difference between the waste pot process and the chilling process is as follows: and (4) recovering and utilizing sensible heat contained in the high-temperature raw gas. In the quench flow gasification technology, crude gas and slag with the temperature up to 1350 ℃ are directly quenched with water to 200 ℃ in a quench chamber. Obviously, a large amount of sensible heat carried by the raw gas and the slag is absorbed and lost by the chilling chamber, a part of physical sensible heat of the raw gas is lost in the chilling process, the sensible heat is about equal to 10% of the lower calorific value, and the water consumption is correspondingly increased. The waste boiler process gasification technology can reduce the temperature of the raw gas from 1350 ℃ to about 400 ℃ at the lowest by a radiation cooler and/or a convection cooler so as to heat the feed water of the boiler and generate a considerable amount of water vapor for users to use. Thus, the efficiency of the hot gas can be improved.
Under the condition that the current environmental protection policy is increasingly tightened, the dry pulverized coal waste boiler flow gasification technology which has high comprehensive energy efficiency, low unit effective gas ratio investment, low water consumption and environmental protection is a main technical means at present. The prior dry coal powder waste boiler flow gasification technology is represented by a shell waste boiler gasification technology, and the cold coal gas efficiency of the technology is 79-81 percent; 10% of the low calorific value of the raw material coal is converted into steam through the convection waste boiler, and the comprehensive thermal efficiency can reach 90%; because the gasification technology uses the quenching gas to chill the high-temperature synthesis gas from 1350 ℃ to 850 ℃, the high-temperature synthesis gas is sent to the convection waste boiler for sensible heat recovery, the heat grade in the temperature range is low, the quenching gas accounts for 60-70% of the generated gas quantity, and the energy consumption is high. On the whole, although the comprehensive thermal efficiency of the shell waste boiler gasification technology is high, the equipment is complex and the investment is expensive, and the input-output ratio is low.
SUMMERY OF THE UTILITY MODEL
The application provides an entrained flow bed gasification equipment adopts radiation waste pot to add the design of convection current waste pot to solve among the prior art shell tablet waste pot gasification technology and synthesize the thermal efficiency high, but the energy consumption is higher, and equipment is complicated and the investment is expensive, and the lower problem of input-output compares, compares in only having radiation waste pot or only having the convection current waste pot technology, and this equipment can produce more steam, can show improvement efficiency and coal utilization ratio.
The technical scheme adopted by the application for solving the technical problems is as follows:
an entrained flow gasification apparatus comprising a gasifier housing comprising a first housing and a second housing disposed on a top region side wall of the first housing;
a slag discharging device, a combustion chamber and a radiation waste boiler are arranged in the first shell, the slag discharging device is connected with a slag discharging port at the bottom of the combustion chamber, and the top end of the combustion chamber is connected with the bottom of the radiation waste boiler through a crude synthesis gas outlet channel;
an air pipe, a convection waste pot and a chilling chamber are arranged in the second shell, the air pipe is communicated with the radiation waste pot, the bottom of the air pipe is connected with the convection waste pot, and the bottom of the convection waste pot is connected with the chilling chamber;
and a plurality of burner devices are uniformly distributed in the bottom area of the combustion chamber along the periphery of the combustion chamber cylinder.
Optionally, the gas-supply pipe includes straight tube section gas-supply pipe and bend pipe section gas-supply pipe, straight tube section gas-supply pipe top with the radiation waste pan is linked together, bend pipe section gas-supply pipe one end is connected the bottom of straight tube section gas-supply pipe, the vertical connection of the other end the convection current waste pan, the central line of convection current waste pan with the central line of bend pipe section gas-supply pipe is tangent.
Optionally, the central lines of the slag discharging device, the combustion chamber and the radiation waste pot are on the same vertical axis, the vertical axis is parallel to the central line of the convection waste pot, and the central line of the convection waste pot and the central line of the chilling chamber are on another vertical axis.
Optionally, the number of the burner devices is 3-6, the burner devices are located on the same horizontal plane at the bottom end of the combustion chamber, and an included angle between a transverse axis of each burner device and a transverse axis of the combustion chamber is 0-6 ℃.
Optionally, the combustion chamber is of a vertical-row cylindrical membrane water-cooled wall structure, the top end and the bottom end of the crude synthesis gas outlet channel are respectively provided with a top cone structure and a bottom cone structure, an included angle α between the top cone structure and the vertical direction is 25-40 ℃, and an included angle between the bottom cone structure and the horizontal direction is 10-20 ℃;
the ratio of the inner diameter D2 of the combustion chamber to the diameter D1 of the slag discharge hole is 3-5:1, and the ratio of the inner diameter D2 of the combustion chamber to the diameter D3 of the outlet channel of the crude synthesis gas is 3-4: 1;
the ratio of the height H1 of the combustion chamber to the inner diameter D2 of the combustion chamber is 2-4:1, and the ratio of the height H2 of the raw synthesis gas outlet channel to the diameter D3 of the raw synthesis gas outlet channel is 1.5-3: 1.
Optionally, the radiation waste boiler is respectively a first cylindrical membrane water-cooled wall and a fin-type membrane water-cooled wall from outside to inside;
the fin type membrane water-cooled wall is composed of 8-24 groups of double-sided water-cooled screens which are uniformly distributed along the radial direction of the cylindrical membrane water-cooled wall, and a rapping dust removal device is arranged outside the first cylindrical membrane water-cooled wall part in the first shell.
Optionally, the included angle gamma between the central line of the straight pipe section gas transmission pipe and the central line of the radiation waste boiler is 30-60 ℃;
the outer wall of the gas transmission pipe is provided with a gas transmission pipe water jacket, and an expansion joint is arranged between the gas transmission pipe water jacket and the second shell.
Optionally, the convection waste boiler is provided with a second cylindrical membrane water-cooled wall and 3-5 groups of spiral coil water-cooled walls from outside to inside, 4-7 circles of water-cooled walls are arranged on the spiral coils of each group of spiral coil water-cooled walls, and a rapping dust removal device is arranged on each group of spiral coils;
an expansion joint is arranged between the second cylindrical membrane water-cooled wall and the gas conveying pipe.
Optionally, the apparatus further comprises a water spraying device, a down pipe and an up pipe, wherein the water spraying device is arranged at the top end of the chilling chamber and connected with the chilling chamber, the down pipe and the up pipe are arranged on the outer wall of the chilling chamber, and the up pipe is arranged on the periphery of the down pipe.
The technical scheme provided by the application comprises the following beneficial technical effects:
the application provides entrained flow gasification equipment which comprises a gasification furnace shell, wherein the gasification furnace shell comprises a first shell and a second shell, and the second shell is arranged on the side wall of the top area of the first shell; a slag discharging device, a combustion chamber and a radiation waste boiler are arranged in the first shell, the slag discharging device is connected with a slag discharging port at the bottom of the combustion chamber, and the top end of the combustion chamber is connected with the bottom of the radiation waste boiler through a crude synthesis gas outlet channel; the inside of the second shell is provided with a gas pipe, a convection waste pot and a chilling chamber, the gas pipe is communicated with the radiation waste pot, the bottom of the gas pipe is connected with the convection waste pot, and the bottom of the convection waste pot is connected with the chilling chamber; the bottom area of the combustion chamber is evenly distributed with a plurality of burner devices along the circumference of the combustion chamber cylinder. By adopting the design of the radiation waste boiler and the convection waste boiler, compared with the technology of only the radiation waste boiler or only the convection waste boiler, the equipment can generate more steam, the energy efficiency and the coal utilization rate can be obviously improved, the lower part of the convection waste boiler is coupled with a chilling chamber, the water-gas ratio can be adjusted according to the requirements of subsequent devices while the crude gas is cooled and dedusted, the process flow is more optimized, and the investment of subsequent equipment such as a Venturi, a carbon washing tower and the like is reduced; simultaneously, a plurality of nozzle devices of evenly distributed around the bottom region edge combustion chamber barrel of combustion chamber compare with single burner device gasification technique, and many nozzle devices can let buggy and oxygen form stronger torrent effect in the gasifier, and the gasifier is easily enlargied, and can not reduce carbon conversion rate. The application provides an entrained flow bed gasification equipment that suitability is strong, and coal utilization ratio and efficiency are high, and process flow is more optimized, has solved among the prior art that the shell tablet waste boiler gasification technology synthesizes the thermal efficiency height, but the energy consumption is higher, and equipment is complicated and the investment is expensive, and the input-output ratio is lower problem.
Drawings
In order to more clearly explain the technical solution of the present application, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious to those skilled in the art that other drawings can be obtained according to the drawings without any creative effort.
FIG. 1 is a schematic structural diagram of an entrained flow gasification apparatus provided in an embodiment of the present application;
FIG. 2 is a top view of a burner arrangement distribution structure provided in an embodiment of the present application;
fig. 3 is a top view of a radiation waste pan structure provided in an embodiment of the present application.
Description of reference numerals:
1-a slag discharging device, 2-a slag discharging port, 3-a burner device, 4-a combustion chamber, 5-a crude synthesis gas outlet channel, 6-a first cylindrical membrane type water cooling wall, 7-a fin type membrane type water cooling wall, 8-a radiation waste boiler, 9-a rapping ash removal device, 10-a gas pipe, 11-an expansion joint, 12-a gas pipe water jacket, 13-a second shell, 14-a convection waste boiler, 15-a second cylindrical membrane type water cooling wall, 16-a spiral coil pipe water cooling wall, 17-a water spraying device, 18-a descending pipe, 19-a chilling chamber, 20-an ascending pipe and 21-a first shell.
Detailed Description
In order to make the technical solutions in the present application better understood by those skilled in the art, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application; it is to be understood that the embodiments described are only a few embodiments of the present application and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
As shown in fig. 1, a schematic structural diagram of an entrained-flow gasification device provided by an embodiment of the present application, the entrained-flow gasification device provided by the embodiment of the present application includes a gasification furnace housing, wherein the housing is an integral protection device wrapped outside the entire device, and for convenience of differentiation, the entire gasification furnace housing is divided into two parts, namely a first housing 21 and a second housing 13, and the second housing 13 is disposed on a side wall of a top region of the first housing 21;
a slag discharging device 1, a combustion chamber 4 and a radiation waste pot 8 are arranged in the first shell 21, the slag discharging device 1 is connected with a slag discharging port 1 at the bottom of the combustion chamber 4, and the top end of the combustion chamber 4 is connected with the bottom of the radiation waste pot 8 through a crude synthesis gas outlet 5;
an air pipe 10, a convection waste pot 14 and a chilling chamber 19 are arranged in the second shell 13, the air pipe 10 is communicated with the radiation waste pot 8, the bottom of the air pipe 10 is connected with the convection waste pot 14, and the bottom of the convection waste pot 14 is connected with the chilling chamber 19;
the bottom area of the combustion chamber 4 is evenly distributed with a plurality of burner devices 3 along the circumference of the cylinder of the combustion chamber 4.
By adopting the design of the radiation waste boiler 8 and the convection waste boiler 14, compared with the technology of only the radiation waste boiler 8 or only the convection waste boiler 14, the equipment can generate more steam, can obviously improve the energy efficiency and the coal utilization rate, the lower part of the convection waste boiler 14 is coupled with a chilling chamber 19, the water-gas ratio can be adjusted according to the requirements of subsequent devices while the crude gas is cooled and dedusted, the process flow is more optimized, and the investment of subsequent equipment such as a Venturi, a carbon washing tower and the like is reduced; simultaneously, a plurality of nozzle devices 3 of evenly distributed around 4 barrels of combustion chamber are followed to the bottom region of combustion chamber 4, compare with 3 gasification techniques of single burner device, and many nozzle devices 3 can let buggy and oxygen form stronger torrent effect in the gasifier, and the gasifier is easily enlargied, and can not reduce carbon conversion rate.
Optionally, the gas pipe 10 comprises a straight pipe section gas pipe 10 and a bent pipe section gas pipe 10, the top of the straight pipe section gas pipe 10 is communicated with the radiation waste boiler 8, one end of the bent pipe section gas pipe 10 is connected with the bottom of the straight pipe section gas pipe 10, the other end of the bent pipe section gas pipe 10 is vertically connected with the convection waste boiler 14, and the central line of the convection waste boiler 14 is tangent to the central line of the bent pipe section gas pipe 10.
The entrained flow gasification technology provided by the embodiment of the application utilizes the radiation waste boiler 8 to be coupled with the convection waste boiler 14 through the air conveying pipe 10 and follow-up chilling process, and the bent pipe section air conveying pipe 10 in the air conveying pipe 10 is connected with the convection waste boiler 14 device, so that the structure of the whole equipment is more reasonable.
Optionally, the central lines of the slag discharging device 1, the combustion chamber 4 and the radiation waste pot 8 are on the same vertical axis, the vertical axis is parallel to the central line of the convection waste pot 14, and the central line of the convection waste pot 14 and the central line of the chilling chamber 19 are on the other vertical axis.
Optionally, the number of the burner devices 3 is 3-6, the burner devices are located on the same horizontal plane at the bottom end of the combustion chamber 4, an included angle between a transverse axis of each burner device 3 and a transverse axis of the combustion chamber 4 is 0-6 ℃, a collision flow field is formed when the included angle is 0 ℃, and a swirling flow field is formed when the included angle is 0-6 ℃, so that reaction power can be increased, as shown in fig. 2, the included angle between the transverse axis of each burner device 3 and the transverse axis of the combustion chamber 4 is 6 ℃.
3-6 burner nozzle devices 3 are arranged on the same horizontal plane at the bottom end of the combustion chamber 4 and are uniformly arranged along the circumference, and the impact flow is used for strengthening the heat and mass transfer process, so that the gas velocity of the cross section in the combustion chamber 4 relatively tends to be uniform.
Optionally, the furnace lining in the combustion chamber 4 is of a vertical-row cylindrical membrane water-cooled wall structure, a SiC protective layer is coated inside the water-cooled wall and can be used for hanging slag, a top cone structure and a bottom cone structure are respectively arranged at the top end and the bottom end of the crude synthesis gas outlet 5, the included angle α between the top cone structure and the vertical direction is 25-40 ℃, the included angle between the bottom cone structure and the horizontal direction is 10-20 ℃, so that liquid slag can be smoothly discharged, and the furnace lining is also of a transition structure of water-cooled wall closing-in;
the ratio of the inner diameter D2 of the combustion chamber 4 to the diameter D1 of the slag discharge port 1 is 3-5:1, and the ratio of the inner diameter D2 of the combustion chamber 4 to the diameter D3 of the outlet position 5 of the crude synthesis gas is 3-4:1, so that the flow rate of the synthesis gas can be ensured;
the ratio between the height H1 of the combustion chamber 4 and the inner diameter D2 of the combustion chamber 4 is 2-4:1, and the ratio between the height H2 of the raw synthesis gas outlet position 5 and the diameter D3 of its raw synthesis gas outlet position 5 is 1.5-3: 1.
Optionally, the radiation waste boiler 8 is respectively a first cylindrical membrane water-cooled wall 6 and a fin-type membrane water-cooled wall 7 from outside to inside, as shown in fig. 3;
the radiation waste heat boiler 8 has different sizes, and the number of the groups of the arranged fin type membrane type water-cooled walls 7 is also different. When the distance between the fin type membrane water-cooling walls 7 is fixed, the larger the radiation waste pot 8 is, the more the number of fin groups is, in the embodiment of the application, the fin type membrane water-cooling walls 7 are set to be 8-24 groups of double-sided water-cooling screens which are uniformly distributed along the radial direction of the cylindrical membrane water-cooling walls, and a rapping dust removal device 9 is arranged outside the first cylindrical membrane water-cooling wall part in the first shell 21;
meanwhile, the bottom of the radiation waste boiler 8 is provided with a water collecting tank, and the top is provided with a gas collecting tank.
A plurality of vibration dust removing devices are arranged outside the first cylindrical film water-cooled wall 6 of the radiation waste boiler 8, and the vibration dust removing devices periodically vibrate the first cylindrical film water-cooled wall to remove the deposited dust on the water-cooled wall.
Optionally, an included angle γ between the center line of the straight pipe section gas pipe 10 and the center line of the radiant waste boiler 8 is 30-60 ℃, wherein the included angle γ is determined according to ash carrying amount and ash viscosity-temperature curve, so that the equipment is guaranteed to be as compact as possible on the premise of no ash adhesion.
The outer wall of the gas pipe 10 is provided with a gas pipe water jacket 12, and an expansion joint 11 is arranged between the gas pipe water jacket 12 and the second shell 13, so that the thermal strain can be balanced, and the thermal stress can be reduced.
Optionally, the convection waste boiler 14 is provided with a second cylindrical membrane water-cooled wall 15 and 3-5 groups of spiral coil water-cooled walls 16 from outside to inside, 4-7 circles of water-cooled walls are arranged on the spiral coils of each group of spiral coil water-cooled walls 16, and in order to avoid serious dust accumulation on the heat exchange surface of the convection waste boiler 14, a rapping dust removal device 9 is arranged on each group of spiral coils;
an expansion joint 11 is arranged between the second cylindrical membrane water-cooling wall 15 and the air conveying pipe 10.
Meanwhile, the bottom of the radiation waste boiler 8 is provided with a water collecting tank, and the top is provided with a gas collecting tank.
Optionally, the apparatus further comprises a water spray device 17, a downcomer 18 and an upcomer 20, the water spray device 17 is arranged at the top end of the quench chamber 19 and is connected with the quench chamber 19, the downcomer 18 and the upcomer 20 are arranged on the outer wall of the quench chamber 19, and the upcomer 20 is arranged at the periphery of the downcomer 18.
After entering the chilling chamber 19, the gas is firstly cooled and washed by the water spray device 17, then enters the chilling chamber 19 through the downcomer 18 for water bath, most of fly ash carried by the crude gas is removed in the chilling chamber 19, and then is defoamed by the riser 20.
Based on the entrained flow bed gasification equipment provided by the embodiment of the application, the embodiment of the application also provides a gasification method of the entrained flow bed gasification equipment, which specifically comprises the following steps:
dry pulverized coal composed of N2Or CO2Dense phase transport enters burner assembly 3 and oxygen and steam also enter burner assembly 3. The coal powder, oxygen and steam are subjected to incomplete oxidation reaction in the combustion chamber 4 to generate CO and H2(90％VDry basis) crude gas as main component, and the gasification temperature is 1300-1700 ℃. The burner devices 3 are distributed on the same horizontal plane at the bottom end of the combustion chamber 4 and are uniformly distributed along the circumference, and the impinging stream is used for strengthening the heat and mass transfer process, so that the gas velocity of the cross section in the combustion chamber 4 relatively tends to be uniform.
Most of the coal ash generated in the combustion chamber 4 flows into the bottom of the combustion chamber 4 in a molten state, and is discharged through the slag discharge device 1.
The raw gas generated by the combustion chamber 4 carries part of coal ash upwards along the central axis of the combustion chamber 4 to enter the raw gas channel of the radiation waste boiler 8. The steam pocket saturated water from outside enters a cylindrical membrane water-cooling wall and a fin-type membrane water-cooling wall 7 of the radiation waste boiler 8 from a water collection tank at the bottom of the radiation waste boiler 8, sensible heat in high-temperature crude gas is absorbed by the water-cooling wall of the radiation waste boiler 8, the temperature of the crude gas is reduced to 600-800 ℃ (the temperature depends on ash characteristics), meanwhile, saturated water in the water-cooling wall absorbs heat and changes phase to generate saturated steam, the saturated steam enters a gas collection tank at the top of the radiation waste boiler 8 from the water-cooling wall of the radiation waste boiler 8 and then enters the steam pocket. The saturated water entering the radiation waste boiler 8 can be subjected to heat exchange in a forced circulation mode or a natural circulation mode. The forced circulation or natural circulation is adopted according to the calculation of the water vapor system. The radiation waste boiler 8 is provided with a vibration dust removing device outside the first cylindrical film water-cooled wall 6, and the first cylindrical film water-cooled wall 6 is periodically vibrated to remove the deposited dust on the water-cooled wall.
The crude gas is cooled by the radiation waste heat boiler 8 and then continuously enters an inclined downward straight pipe section in the gas transmission pipe 10. The gas line 10 is protected by a membrane water wall and is a high pressure boiler feed water heater (similar to an economizer in a circulating fluidized bed). The high-pressure boiler feed water is pumped to the gas pipe 10 from the outside, heated by high-temperature crude gas and sent to the steam pocket.
The raw gas enters the convection waste boiler 14 through the gas conveying pipe 10, and the high-pressure saturated water of the steam pocket from the outside enters the water collecting tank from the bottom of the convection waste boiler 14 and further enters the cylindrical water-cooled wall and the spiral coil water-cooled wall. The temperature of the crude gas in the convection waste boiler 14 is further reduced to 350-600 ℃, the temperature depends on subsequent products, and the different temperatures lead the temperature of the synthesis gas and the water-gas ratio of the obtained device to be different so as to meet the requirements of the subsequent devices. Meanwhile, a byproduct of 10.0MPa saturated steam on a water-cooled wall of the convection waste boiler 14 enters a gas collection tank at the top of the convection waste boiler 14 and then enters a steam pocket. The saturated water entering the convection waste boiler 14 can be subjected to heat exchange in a forced circulation manner or in a natural circulation manner. The forced circulation or natural circulation is adopted according to the calculation of the water vapor system.
After entering the chilling chamber 19 through the bottom of the convection waste boiler 14, the crude gas is firstly cooled and washed by chilling water and then enters the chilling chamber 19 through the downcomer 18 for water bath, and most of fly ash carried by the crude gas is removed in the chilling chamber 19. Then the foam is removed through the riser 20. The temperature of the synthetic gas in the chilling chamber 19 is reduced to 160-220 ℃, and the temperature and the water-gas ratio of the synthetic gas of the obtained device are different due to different temperatures so as to meet the requirements of the subsequent device. And a plurality of vibration dust removing devices are arranged outside the cylindrical water-cooled wall of the convection waste boiler 14, and the vibration dust removing devices periodically vibrate the cylindrical water-cooled wall to remove the deposited dust on the water-cooled wall.
And (4) sending the synthesis gas subjected to dust removal to a subsequent device from a synthesis gas outlet, and adjusting the temperature and the water-gas ratio of the synthesis gas to the state required by the subsequent device.
It is noted that relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that an article or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The above description is merely exemplary of the present application and is presented to enable those skilled in the art to understand and practice the present application. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the application. Thus, the present application is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
It will be understood that the present application is not limited to what has been described above and shown in the accompanying drawings, and that various modifications and changes can be made without departing from the scope thereof. The scope of the application is limited only by the appended claims.
Claims (9)
1. An entrained flow gasification device is characterized by comprising a gasification furnace shell, wherein the gasification furnace shell comprises a first shell and a second shell, and the second shell is arranged on the side wall of the top area of the first shell;
a slag discharging device, a combustion chamber and a radiation waste boiler are arranged in the first shell, the slag discharging device is connected with a slag discharging port at the bottom of the combustion chamber, and the top end of the combustion chamber is connected with the bottom of the radiation waste boiler through a crude synthesis gas outlet channel;
an air pipe, a convection waste pot and a chilling chamber are arranged in the second shell, the air pipe is communicated with the radiation waste pot, the bottom of the air pipe is connected with the convection waste pot, and the bottom of the convection waste pot is connected with the chilling chamber;
and a plurality of burner devices are uniformly distributed in the bottom area of the combustion chamber along the periphery of the combustion chamber cylinder.
2. The entrained-flow bed gasification equipment as recited in claim 1, wherein the gas delivery pipe comprises a straight pipe section gas delivery pipe and an elbow pipe section gas delivery pipe, the top of the straight pipe section gas delivery pipe is communicated with the radiation waste boiler, one end of the elbow pipe section gas delivery pipe is connected with the bottom of the straight pipe section gas delivery pipe, the other end of the elbow pipe section gas delivery pipe is vertically connected with the convection waste boiler, and the center line of the convection waste boiler is tangent to the center line of the elbow pipe section gas delivery pipe.
3. An entrained flow gasification apparatus as recited in claim 1, wherein the centerline of the slagging device, combustion chamber and radiant fryer are on the same vertical axis, the vertical axis being parallel to the centerline of the convection fryer, the centerline of the convection fryer being on another vertical axis than the centerline of the quench chamber.
4. An entrained-flow gasification device as recited in claim 1, wherein the number of the burner devices is 3-6, the burner devices are located on the same horizontal plane at the bottom end of the combustion chamber, and the included angle between the transverse axis of the burner devices and the transverse axis of the combustion chamber is 0-6 ℃.
5. An entrained-flow gasification device according to claim 1, wherein the combustion chamber is a vertical-row cylindrical membrane water-cooled wall structure, the top end and the bottom end of the raw synthesis gas outlet channel are respectively provided with a top cone structure and a bottom cone structure, the included angle α between the top cone structure and the vertical direction is 25-40 ℃, and the included angle between the bottom cone structure and the horizontal direction is 10-20 ℃;
the ratio of the inner diameter D2 of the combustion chamber to the diameter D1 of the slag discharge hole is 3-5:1, and the ratio of the inner diameter D2 of the combustion chamber to the diameter D3 of the outlet channel of the crude synthesis gas is 3-4: 1;
the ratio of the height H1 of the combustion chamber to the inner diameter D2 of the combustion chamber is 2-4:1, and the ratio of the height H2 of the raw synthesis gas outlet channel to the diameter D3 of the raw synthesis gas outlet channel is 1.5-3: 1.
6. An entrained flow gasification plant as recited in claim 1, wherein the radiant syngas cooler is, from outside to inside, a first tubular membrane water wall and a fin type membrane water wall, respectively;
the fin type membrane water-cooled wall is composed of 8-24 groups of double-sided water-cooled screens which are uniformly distributed along the radial direction of the cylindrical membrane water-cooled wall, and a rapping dust removal device is arranged outside the first cylindrical membrane water-cooled wall part in the first shell.
7. An entrained-flow bed gasification device as recited in claim 2, wherein an included angle γ between a center line of the straight pipe section gas transmission pipe and a center line of the radiation waste boiler is 30-60 ℃;
the outer wall of the gas transmission pipe is provided with a gas transmission pipe water jacket, and an expansion joint is arranged between the gas transmission pipe water jacket and the second shell.
8. An entrained-flow gasification device as recited in claim 1, wherein the convection waste boiler is provided with a second cylindrical membrane water-cooled wall and 3-5 sets of spiral coil water-cooled walls from outside to inside, 4-7 turns of water-cooled walls are provided on the spiral coils of each set of spiral coil water-cooled walls, and a rapping ash removal device is provided on each set of spiral coils;
an expansion joint is arranged between the second cylindrical membrane water-cooled wall and the gas conveying pipe.
9. The entrained-flow gasification apparatus of claim 1, further comprising a water spray device disposed at a top end of the quench chamber and connected thereto, a downcomer and a riser disposed on an outer wall of the quench chamber, the riser being disposed at a periphery of the downcomer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921511653.0U CN210506234U (en) | 2019-09-11 | 2019-09-11 | Entrained flow bed gasification equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921511653.0U CN210506234U (en) | 2019-09-11 | 2019-09-11 | Entrained flow bed gasification equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210506234U true CN210506234U (en) | 2020-05-12 |
Family
ID=70569349
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921511653.0U Active CN210506234U (en) | 2019-09-11 | 2019-09-11 | Entrained flow bed gasification equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210506234U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110484299A (en) * | 2019-09-11 | 2019-11-22 | 宁夏神耀科技有限责任公司 | A kind of entrained flow gasification equipment |
-
2019
- 2019-09-11 CN CN201921511653.0U patent/CN210506234U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110484299A (en) * | 2019-09-11 | 2019-11-22 | 宁夏神耀科技有限责任公司 | A kind of entrained flow gasification equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108410510B (en) | Integrated coal gasifier for ash removal of waste boiler | |
| CN106433790B (en) | Gasification equipment with heat recovery device and capable of preventing slag blockage | |
| CN202744505U (en) | Chiller and gasification furnace with same | |
| CN105586093B (en) | The gasification reactor and its gasification process of a kind of band part waste-heat recovery device | |
| CN107090311A (en) | High efficient heat recovery carries flow gasification stove | |
| CN103160329B (en) | Coal water slurry water wall gasification furnace of waste heat boiler process | |
| CN108342227B (en) | Synthetic gas sensible heat recovery device and recovery method and gasifier | |
| CN108130133B (en) | Large-scale semi-waste boiler gasification device | |
| CN102786992B (en) | Radiation heat-convection integrated synthesis gas cooler | |
| CN104629807A (en) | Chilling process gasifier with high-temperature heat recovery unit | |
| CN203174051U (en) | Coal water slurry water-cooled wall gasification furnace in waste boiler process | |
| CN108102719A (en) | A kind of gasification furnace for preventing slagging and thermal energy high efficiente callback | |
| CN106867590A (en) | A kind of useless pot Quench integral type water-coal-slurry water cooled wall gasification furnace and gasification process | |
| CN206706032U (en) | A kind of useless pot Quench integral type water-coal-slurry water cooled wall gasification furnace | |
| CN105154140B (en) | A kind of method and apparatus for the multistage air-flow bed coal-gasification for coupling high temperature shift | |
| CN210506234U (en) | Entrained flow bed gasification equipment | |
| CN104531222B (en) | Pyrolysis of coal system and method using spouted bed reactor | |
| CN110564456A (en) | gasification furnace with radiation waste boiler | |
| WO2020006994A1 (en) | Gasifier employing radiant heat exchange technique and gasification method | |
| CN211497525U (en) | Gasifier capable of efficiently recovering energy | |
| CN202754974U (en) | Internal heat exchange type hydrogenation gasification furnace | |
| CN110484299A (en) | A kind of entrained flow gasification equipment | |
| CN103965966B (en) | A kind of dry powder pressurizing gasifying apparatus with treatment of Organic Wastewater | |
| CN110655956A (en) | Hazardous waste gas chemical treatment system | |
| CN210656823U (en) | Gasification furnace with radiation waste boiler |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |