CN209836098U - Supercritical water circulating fluidized bed gasification system - Google Patents
Supercritical water circulating fluidized bed gasification system Download PDFInfo
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- CN209836098U CN209836098U CN201920609466.XU CN201920609466U CN209836098U CN 209836098 U CN209836098 U CN 209836098U CN 201920609466 U CN201920609466 U CN 201920609466U CN 209836098 U CN209836098 U CN 209836098U
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Abstract
The utility model discloses a supercritical water circulating fluidized bed gasification system, including first water tank, first high-pressure plunger pump, second high-pressure plunger pump, third high-pressure plunger pump, arrange the sediment pump, return material pump, storage tank, first charging means, second charging means, arrange the sediment ware, arrange sediment cooler, riser, cyclone, riser, return material valve, pulse damper, regenerator, cooler, pre-heater, back pressure valve, vapour and liquid separator, wet-type gas flowmeter, second water tank, cooling tower, cooling water pump and a plurality of valve, temperature pressure observing and controlling system. The utility model adopts the supercritical water circulating fluidized bed as the reactor, compared with the bubbling fluidized bed, the reactor has higher operation gas velocity, can realize the gasification of high gas velocity, high coal flux and high coal concentration, and greatly improves the efficiency and the capacity of the gasification furnace; meanwhile, the bed layer is approximately bubble-free, the influence of the geometrical structure of the gasification furnace is reduced, and the device is easy to enlarge in large scale.
Description
Technical Field
The utility model belongs to the clean conversion of coal and renewable resources utilizes the field, in particular to supercritical water circulating fluidized bed gasification system.
Background
The traditional utilization mode of coal for a long time causes pollution which is difficult to reverse for natural environments such as atmosphere and the like, and seriously threatens and influences the physical health of residents. Therefore, the research and development of clean coal technology can improve the utilization efficiency of coal and reduce pollution emission, and has important strategic significance for realizing the coordinated development of economy, energy and environment.
The supercritical water gasification technology can directly treat coal with high moisture content and convert the coal into hydrogen-rich gas, has the advantages of high gasification rate, high gasification speed, high hydrogen content, strong raw material adaptability and the like, is widely concerned by domestic and foreign scholars, and is rapidly developed in the past decades. MIT's model firstly carried out the gasification research of coal, biomass etc. in supercritical water kettle-type reactor, showed the good prospect of supercritical water gasification of coal to applied for patent (US4113446), but its batch reactor that adopts is mainly used for the research in the aspect of reaction mechanism, can not satisfy the demand of this technological industrialization in the future. In 2002, the subject group is utility model discloses a supercritical water gasification hydrogen production method and device (ZL02114529.6) of organic solid raw materials, solves the key technical problem of high-pressure multiphase continuous conveying of high-concentration materials, realizes the complete gasification of raw materials such as coal, biomass and the like in a pipe flow reactor, but the pipe flow reactor is easy to have wall slagging and blockage, and leads to system halt. In 2005, the subject group made practical a device and method (ZL200510041633.8) for producing hydrogen by coal and biomass co-supercritical water gasification, which solved the technical problem of rapid temperature rise of reaction materials and realized high-efficiency gasification of high-concentration coal. In 2007, the subject group is utility model of a coal and biomass supercritical water fluidized bed gasification/partial oxidation hydrogen production device and method (ZL200710017691.6), which solves the difficult problem of slagging and blocking of the tubular reactor, realizes high-efficiency gasification of high-concentration biomass, but the operation can only be performed at medium and low gas speeds, and belongs to a bubbling fluidized bed from the view of two-phase flow state, although the difficult problem of slagging and blocking of the tubular reactor can be solved, and the high-efficiency gasification of high-concentration biomass and coal can be realized, similar to the traditional bubbling fluidized bed, some important parameters in the reactor, such as bed expansion, gas-solid mixing, bubble characteristics, heat transfer characteristics, mass transfer characteristics of reaction gas, etc., strongly depend on the size of the reactor. The bubbling action of a bubbling fluidized bed also presents problems of reduced reactor efficiency and difficult reactor upscaling.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome above-mentioned difficult problem, provide a supercritical water circulating fluidized bed gasification system, this system and method can make the operation gas velocity higher, can realize the gasification of high gas velocity and high flux, and the bed is approximate bubble-free, has improved the efficiency and the ability of fluidized bed greatly to the reactor easily enlargies.
The utility model discloses a realize through following technical scheme:
a supercritical water circulating fluidized bed gasification system comprises a circulating fluidized bed subsystem, a feeding subsystem, a heating subsystem and a gas taking subsystem;
the circulating fluidized bed subsystem comprises a lifting pipe, a cyclone separator and a return material conveying device, wherein the lifting pipe is used as a gasification furnace body, the bottom of the lifting pipe is provided with a supercritical water inlet, the lower part of the lifting pipe is provided with a feed inlet and a return material port, an outlet at the upper part of the lifting pipe is connected with the inlet of the cyclone separator, a discharge port at the bottom of the cyclone separator is connected with the return material port of the lifting pipe through the return material conveying device, and the cyclone separator is provided with an;
the feeding subsystem conveys gasification raw materials to the lifting pipe through a feeding hole of the lifting pipe;
the heat subsystem conveys supercritical water to the riser through a supercritical water inlet of the riser, and cools a mixture of the supercritical water and gas discharged from an exhaust port of the cyclone separator, so that the supercritical water is cooled into liquid water;
the gas taking subsystem is used for separating and collecting liquid water and gas cooled by the heat subsystem.
Preferably, the return material conveying device comprises a vertical pipe, a return material valve and a return material pump; the bottom discharge port of the cyclone separator is connected with the inlet at the upper part of the material returning valve through a vertical pipe, the outlet at the lower part of the material returning valve is connected with the material returning port of the lifting pipe, and the material returning pressure inlet at the lower part of the material returning valve is connected with the material returning pump.
Preferably, the feeding subsystem comprises a first water tank, a storage tank, a first feeder, a second high-pressure plunger pump and a third high-pressure plunger pump; the material storage tank is provided with a gas inlet, a material inlet and an outlet, the outlet of the material storage tank is divided into two paths and is respectively connected with the inlets of the first feeder and the second feeder, and the outlets of the first feeder and the second feeder are converged and then connected with the feed inlet of the lifting pipe; the upper parts of the first feeder and the second feeder are connected through a pipeline; the outlet of the first water tank is divided into two paths and is respectively connected with the inlets of the second high-pressure plunger pump and the third high-pressure plunger pump; the outlet of the second high-pressure plunger pump is connected with the upper parts of the first feeder and the second feeder, the outlet of the third high-pressure plunger pump is divided into three paths, one path is connected with the upper part of the first feeder, the other path is connected with the upper part of the second feeder, and the other path is connected with the feed inlet of the lifting pipe.
Preferably, the thermal subsystem comprises a first water tank, a heat regenerator, a cooler and a preheater; a hot fluid inlet of the heat regenerator is connected with an exhaust port of the cyclone separator, a hot fluid outlet of the heat regenerator is connected with a hot fluid inlet of the cooler, and a hot fluid outlet of the cooler is connected with the gas taking subsystem through a back pressure valve; the first water tank is connected with a cold fluid inlet of the heat regenerator through a first high-pressure plunger pump, a cold fluid outlet of the heat regenerator is connected with an inlet of the preheater, and an outlet of the preheater is connected with a supercritical water inlet of the lifting pipe.
The first water tank is connected with an inlet of the pulse damper through a first high-pressure plunger pump, an outlet of the pulse damper is divided into two paths, one path is connected with a cold fluid inlet of the heat regenerator, and the other path is connected with a hot fluid outlet of the cooler.
Further, the cooling system also comprises a second water tank, a cooling water pump and a cooling tower; the second water tank is connected with a cooling water inlet of the cooler through a cooling water pump, a cooling water outlet of the cooler is connected with a cooling tower inlet, and a cooling tower outlet is connected with the second water tank.
Preferably, the gas taking subsystem comprises a gas-liquid separator, a wet gas flowmeter and a gas taking bag, and a hot fluid outlet of the cooler is connected with an inlet of the gas-liquid separator; the gas outlet of the gas-liquid separator is divided into two paths, one path is connected with the wet gas flowmeter, and the other path is connected with the gas bag.
Preferably, the system also comprises a slag discharging subsystem, wherein the slag discharging subsystem comprises a first water tank, a slag discharging pump, a slag discharging device and a slag discharging cooler; the lower part of the lifting pipe is provided with a slag discharge port, the first water tank is connected with a water inlet of a slag discharge device through a slag discharge pump, the slag discharge port of the lifting pipe is connected with an inlet of a slag discharge cooler, an outlet of the slag discharge cooler is connected with a waste residue inlet of the slag discharge device, and the bottom of the slag discharge device is provided with a slag discharge port.
Compared with the prior art, the utility model discloses following profitable technological effect has:
when the utility model is used, unreacted gasification raw materials are carried out of the riser by supercritical water and enter the cyclone separator, and after separation by the cyclone separator, the mixture of the supercritical water and gas generated by reaction is discharged from the exhaust port of the cyclone separator, enters the thermal subsystem for cooling, and then is separated and collected by the gas taking subsystem; the unreacted gasification raw material separated by the cyclone separator returns to the lift pipe through the material returning and conveying device to continue to participate in the reaction. Higher operating gas velocities can be used because unreacted gasification feedstock can be recycled to the riser. Under the state of fast fluidization, the bed layer is approximately bubble-free, on one hand, the high gas-solid slip speed strengthens the interphase transmission, improves the reaction speed, ensures that the material distribution and the temperature distribution in the lifting pipe are more uniform, is beneficial to the reaction, can realize the gasification of high gas velocity, high gasification raw material flux and high gasification raw material concentration, and greatly improves the efficiency and the capacity of the gasification furnace; on the other hand, the contact between gasification raw material particles and supercritical water is greatly strengthened, the influence of the geometrical structure of the gasification furnace is reduced, and the device is easy to enlarge in size. The utility model adopts the supercritical water circulating fluidized bed as the reactor, thereby avoiding the problem of slagging and blocking of the pipe flow reactor; compared with a bubbling fluidized bed, the circulating fluidized bed has higher operation gas velocity, can realize the gasification of high gas velocity, high gasification raw material flux and coal concentration of gasification raw materials, and greatly improves the efficiency and the capacity of the gasification furnace. The utility model provides a new technology of supercritical water circulating fluidized bed (fast fluidization) gasification improves the efficiency and the throughput of single reactor.
Furthermore, a return valve is connected with a return pump, and the return pump is used for inflating the return valve, so that unreacted raw materials are enabled to return to the lifting pipe, and the structure is simple.
Furthermore, through setting up two charging means, when a charging means feeding, another charging means can be reinforced, and two charging means go on in turn, can realize the long-time continuous steady operation of fluidized bed.
Furthermore, in the heat regenerator, cold water in the first water tank enters the heat regenerator through the first high-pressure plunger pump and the damping buffer to recover heat of high-temperature fluid after reaction so as to realize preliminary temperature rise, reduce the heating power required by the preheater and improve the energy utilization efficiency of the whole system.
Furthermore, the slag discharge system can discharge waste slag in the riser in time, so that the fluidized bed can continuously and stably run for a long time.
Drawings
FIG. 1 is a system flow chart of the supercritical water circulating fluidized bed coal gasifier of the present invention.
The reference numbers in the figures are: 1-a first water tank, 2-a first high-pressure plunger pump, 3-a second high-pressure plunger pump, 4-a third high-pressure plunger pump, 5-a slag discharge pump, 6-a return pump, 7-a material storage tank, 8-a first feeder, 9-a second feeder, 10-a slag discharge device, 11-a slag discharge cooler, 12-a lifting pipe, 13-a cyclone separator, 14-a vertical pipe, 15-a return valve, 16-a pulse damper, 17-a heat regenerator, 18-a cooler, 19-a preheater, 20-a back pressure valve, 21-a gas-liquid separator, 22-a wet gas flowmeter, 23-a second water tank, 24-a cooling tower and 25-a cooling water pump.
Detailed Description
The present invention will now be described in further detail with reference to specific examples, which are intended to be illustrative, but not limiting, of the invention.
As shown in FIG. 1, the supercritical water circulating fluidized bed gasification system comprises a circulating fluidized bed subsystem, a feeding subsystem, a deslagging subsystem, a thermal subsystem and a gas taking subsystem.
The circulating fluidized bed subsystem comprises a lifting pipe 12, a cyclone separator 13, a vertical pipe 14, a material returning valve 15 and a material returning pump 6, wherein the lifting pipe 12 is a gasification furnace body. The bottom of the lifting pipe 12 is provided with a supercritical water inlet which is connected with the outlet of a preheater 19; the lower part of the lifting pipe 12 is provided with a slag discharge port which is connected with a slag discharge subsystem; the middle lower part of the lifting pipe 12 is provided with a feeding hole which is connected with a feeding subsystem. An outlet at the upper part of the lifting pipe 12 is connected with an inlet of a cyclone separator 13 through a connecting pipeline, an exhaust outlet of the cyclone separator 13 is connected with a hot fluid inlet of a heat regenerator 17, the cyclone separator 13 is directly connected with a vertical pipe 14 and the vertical pipe 14 is directly connected with a material returning valve 15 through welding respectively, so that a discharge port at the bottom of the cyclone separator 13 is connected with an inlet at the upper part of the material returning valve 15 through the vertical pipe 14, an outlet at the lower part of the material returning valve 15 is connected with a material returning port at the lower part of the lifting pipe 12, and a material returning pressure inlet at the lower part of the material returning valve 15 is connected. The return pump 6 adopts a high-pressure plunger pump and is used for introducing high-temperature and high-pressure water into the return valve 15 from a return pressure inlet so as to push the material in the return valve 15 to return to the lifting pipe 12.
The feeding subsystem comprises a first water tank 1, a storage tank 7, a first feeder 8, a second feeder 9, a second high-pressure plunger pump 3 and a third high-pressure plunger pump 4; the storage tank 7 is provided with a gas inlet, a material inlet and an outlet, the outlet of the storage tank 7 is divided into two paths which are respectively connected with the inlets of the first feeder 8 and the second feeder 9, and the outlets of the first feeder 8 and the second feeder 9 are converged and then connected with the feed inlet of the lifting pipe 12. The first feeder 8, the second feeder 9, the second high-pressure plunger pump 3 and the third high-pressure plunger pump 4 are connected with each other through pipelines and valves; specifically, the upper parts of a first feeder 8 and a second feeder 9 are connected with a valve through a pipeline, the outlet of a first water tank 1 is divided into two paths which are respectively connected with the inlets of a second high-pressure plunger pump 3 and a third high-pressure plunger pump 4, the outlet of the second high-pressure plunger pump 3 is connected with the upper parts of the first feeder 8 and the second feeder 9, the outlet of the third high-pressure plunger pump 4 is divided into three paths, one path is connected with the upper part of the first feeder 8, the other path is connected with the upper part of the second feeder 9, and the other path is directly connected with a feed inlet of a lifting pipe 12.
The slag discharging subsystem comprises a first water tank 1, a slag discharging pump 5, a slag discharging device 10 and a slag discharging cooler 11, wherein the first water tank 1 is connected with a water inlet of the slag discharging device 10 through the slag discharging pump 5, a slag discharging port of the lifting pipe 12 is connected with an inlet of the slag discharging cooler 11, an outlet of the slag discharging cooler 11 is connected with a waste slag inlet of the slag discharging device 10, and a slag discharging port is arranged at the bottom of the slag discharging device 10.
The thermal subsystem mainly comprises a first water tank 1, a heat regenerator 17, a cooler 18, a preheater 19, a second water tank 23, a cooling water pump 25 and a cooling tower 24. The hot fluid inlet of the heat regenerator 17 is connected with the exhaust port of the cyclone separator 13, the hot fluid outlet of the heat regenerator 17 is connected with the hot fluid inlet of the cooler 18, the hot fluid outlet of the cooler 18 is connected with the inlet of the backpressure valve 20, and the outlet of the backpressure valve 20 is connected with the gas taking subsystem. The second water tank 23 is connected to a cooling water inlet of the cooler 18 by a cooling water pump 25, a cooling water outlet of the cooler 18 is connected to an inlet of the cooling tower 24, and an outlet of the cooling tower 24 is connected to the second water tank 23. First water tank 1 links to each other through first high-pressure plunger pump 2 and 16 entrys of pulse damper, 16 exports of pulse damper and regenerator 17's cold fluid entry linkage, and regenerator 17's cold fluid export and preheater 19's entry linkage, preheater 19's export and the supercritical water entry linkage of riser 12.
The gas taking subsystem comprises a gas-liquid separator 21, a wet gas flowmeter 22 and a gas taking bag. The outlet of the back pressure valve 20 is connected with the inlet of the gas-liquid separator 21; one path of the gas outlet of the gas-liquid separator 21 is connected with the wet gas flowmeter 22 through a three-way valve, and the other path is connected with a gas bag.
The bottom end cap of the riser 12 is equipped with a graphite wound gasket and an air distribution plate to ensure effective sealing of the end cap and uniform distribution of the inlet fluid. The riser 12 is electrically heated to maintain the temperature required for gasification, six K-type thermocouples are used for measuring the fluid temperature at different heights of the riser, and a pressure sensor is used for measuring the system pressure.
The utility model discloses adopt the supplementary coal particle fluidization of quartz sand granule during the use, the particle size scope of gasification raw material granule is 0 ~ 200 mu m, the particle size scope 10 ~ 80 mu m of quartz sand granule, and supercritical water mass flow is 30 ~ 220 kg/h.
Hot fluid at the outlet of the preheater 19 passes through the lifting pipe 12 from bottom to top, so that quartz sand in the lifting pipe 12 is in a fast fluidized state; the normal temperature gasification raw material enters the lifting pipe 12 from a feeder (8 or 9) through a feed inlet at the middle lower part of the lifting pipe 12, and is mixed with hot fluid and quartz sand particles in the lifting pipe 12 to realize rapid temperature rise.
The heat regenerator and the cooler are both sleeve type heat exchangers arranged in a countercurrent mode and are made of 304 stainless steel; the riser is made of Inconel 625, the system pressure is up to 30MPa, and the temperature is up to 700 ℃.
Supercritical water circulating fluidized bed gasification system, concrete working process as follows: quartz sand particles with the particle size range of 10-80 mu m are added into the riser 12 in advance and used as bed materials to assist the fluidization of the coal particles. Meanwhile, coal is prepared into coal slurry with required concentration and added into the storage tank 7, and the coal slurry is pressed into the first charging device 8 and/or the second charging device 9 by using N2 with certain pressure. The first high pressure plunger pump 2 is turned on, its mass flow is adjusted to a predetermined value, and the back pressure valve 20 is adjusted to bring the system to a predetermined pressure. Preheater 19 and the heating means of riser 12 are activated to bring the temperature of the fluid in reactor riser 12 to a predetermined value. The second high-pressure plunger pump 3 and the third high-pressure plunger pump 4 are turned on to raise the pressure of the first doser 8 and the second doser 9 to the system pressure. And adjusting the mass flow of the third high-pressure plunger pump 4 to a preset value, and simultaneously opening a lower outlet valve of a feeder (8 or 9) to press the coal slurry into the riser 12 for reaction. Under the fast fluidization operation of riser 12, quartz sand particles and unreacted coal particles are carried out of riser 12 by supercritical water and enter cyclone 13. After separation by the cyclone separator 13, a mixture of supercritical water and gas generated by reaction is discharged from an exhaust port of the cyclone separator 13, enters the heat regenerator 17 to exchange heat with cold fluid, then enters the cooler 18 to be cooled to normal temperature, enters the gas-liquid separator 21 after passing through the backpressure valve 20, and the yield of the gas separated by the gas-liquid separator 21 is measured by the wet gas flowmeter 22; the quartz sand particles and unreacted coal particles separated by the cyclone separator 13 enter a return valve 15 through a vertical pipe 14, and are sent back to the riser pipe 12 to continuously participate in fluidization or reaction under the action of return air provided by the return pump 6. The residue produced by the reaction was discharged through a slag discharge system, and the gas composition was analyzed by gas chromatography.
The supercritical water circulating fluidized bed gasification method comprises the following steps: adjusting the pressure and temperature of the system to preset pressure and temperature, feeding slurry prepared from gasification raw materials into a lifting pipe through a feeding hole of the lifting pipe, feeding supercritical water generated by a thermal subsystem into the lifting pipe through a supercritical water inlet of the lifting pipe at a flow speed of 30-220 kg/h, taking unreacted gasification raw materials out of the lifting pipe by the supercritical water, feeding the gasification raw materials into a cyclone separator, separating by the cyclone separator, discharging a mixture of the supercritical water and gas generated by reaction from an exhaust port of the cyclone separator, feeding the mixture into the thermal subsystem for cooling, and separating and collecting liquid water and gas by a gas taking subsystem; the unreacted gasification raw material separated by the cyclone separator returns to the lift pipe through the material returning and conveying device to continue to participate in the reaction.
The utility model discloses can operate under the high flow rate, the flow rate can reach 30 ~ 220kg/h, under the fast fluidization state, the bed is approximate bubble-free, on the one hand high gas-solid slip speed, has reinforceed alternate transmission, improves reaction rate, makes material distribution and temperature distribution more even in the riser, is favorable to going on of reaction, can realize the gasification of high gas velocity, high gasification raw materials flux and high gasification raw materials concentration, has improved the efficiency and the ability of gasifier greatly; on the other hand, the contact between gasification raw material particles and supercritical water is greatly strengthened, the influence of the geometrical structure of the gasification furnace is reduced, and the device is easy to enlarge in size.
The utility model discloses a supercritical water circulating fluidized bed is as the reactor, compares in bubbling fluidized bed, has higher operation gas velocity, and the quartz sand granule that is in fast fluidization in the reactor can strengthen the heat and mass transfer in the reactor, makes normal atmospheric temperature material and supercritical water and bed material quick mixing, realizes the rapid heating up of coal, can make coal granule and supercritical water fully contact, realizes the high-efficient gasification of high concentration coal, can realize the gasification of high gas velocity, high coal flux and high coal concentration, can improve the efficiency and the ability of gasifier greatly; meanwhile, in a fast fluidized state, the bed layer is nearly bubble-free, the influence of the geometrical structure of the gasification furnace is reduced, and the device is easy to enlarge in large scale.
The system can be used for researching the influence of coal granularity, coal slurry concentration, slurry flow, preheating water temperature, reactor pressure, preheating water flow, initial storage amount, quartz sand particle size, return air quantity and the like on the gasification reaction of coal in the supercritical water circulating fluidized bed. Further, the influence of different material returning port heights, material returning valve types and the like on gasification can be continuously researched by replacing different material returning valves.
The gasification raw material in the utility model can be coal, and also can be primary biomass or biomass model compound.
The above examples are merely illustrative of the present invention and are not intended to limit the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A supercritical water circulating fluidized bed gasification system is characterized by comprising a circulating fluidized bed subsystem, a feeding subsystem, a heating subsystem and a gas taking subsystem;
the circulating fluidized bed subsystem comprises a lifting pipe (12), a cyclone separator (13) and a return material conveying device, wherein the lifting pipe (12) is used as a gasification furnace body, a supercritical water inlet is formed in the bottom of the lifting pipe (12), a feed inlet and a return material port are formed in the lower portion of the lifting pipe (12), an outlet in the upper portion of the lifting pipe (12) is connected with the inlet of the cyclone separator (13), a discharge port in the bottom of the cyclone separator (13) is connected with the return material port of the lifting pipe (12) through the return material conveying device, and an exhaust port is formed in the cyclone separator (13);
the feeding subsystem conveys gasification raw materials to the lifting pipe (12) through a feeding hole of the lifting pipe (12);
the thermal subsystem conveys supercritical water to the lifting pipe (12) through a supercritical water inlet of the lifting pipe (12), and cools a mixture of the supercritical water and gas discharged from an exhaust port of the cyclone separator (13) to cool the supercritical water into liquid water;
the gas taking subsystem is used for separating and collecting liquid water and gas cooled by the heat subsystem.
2. The supercritical water circulating fluidized bed gasification system of claim 1, characterized in that the return material delivery device comprises a riser (14), a return material valve (15) and a return material pump (6); a discharge port at the bottom of the cyclone separator (13) is connected with an inlet at the upper part of a material returning valve (15) through a vertical pipe (14), an outlet at the lower part of the material returning valve (15) is connected with a material returning port of the lifting pipe (12), and a material returning pressure inlet at the lower part of the material returning valve (15) is connected with a material returning pump (6).
3. The supercritical water circulating fluidized bed gasification system of claim 1, wherein the charging subsystem comprises a first water tank (1), a storage tank (7), a first charger (8), a second charger (9), a second high-pressure plunger pump (3) and a third high-pressure plunger pump (4); the material storage tank (7) is provided with a gas inlet, a material inlet and a material outlet, the outlet of the material storage tank (7) is divided into two paths to be respectively connected with the inlets of the first feeder (8) and the second feeder (9), and the outlets of the first feeder (8) and the second feeder (9) are converged and then connected with the feed inlet of the lifting pipe (12); the upper parts of the first feeder (8) and the second feeder (9) are connected through a pipeline; the outlet of the first water tank (1) is divided into two paths and is respectively connected with the inlets of the second high-pressure plunger pump (3) and the third high-pressure plunger pump (4); the outlet of the second high-pressure plunger pump (3) is connected with the upper parts of the first feeder (8) and the second feeder (9), the outlet of the third high-pressure plunger pump (4) is divided into three paths, one path is connected with the upper part of the first feeder (8), the other path is connected with the upper part of the second feeder (9), and the other path is connected with the feed inlet of the lifting pipe (12).
4. Supercritical water circulating fluidized bed gasification system according to claim 1, characterized by a thermal subsystem comprising a first water tank (1), a regenerator (17), a cooler (18) and a preheater (19); a hot fluid inlet of the heat regenerator (17) is connected with an exhaust port of the cyclone separator (13), a hot fluid outlet of the heat regenerator (17) is connected with a hot fluid inlet of the cooler (18), and a hot fluid outlet of the cooler (18) is connected with the gas taking subsystem through a backpressure valve (20); the first water tank (1) is connected with a cold fluid inlet of the heat regenerator (17) through the first high-pressure plunger pump (2), a cold fluid outlet of the heat regenerator (17) is connected with an inlet of the preheater (19), and an outlet of the preheater (19) is connected with a supercritical water inlet of the lifting pipe (12).
5. The supercritical water circulating fluidized bed gasification system of claim 4, further comprising a pulse damper (16), wherein the first water tank (1) is connected with an inlet of the pulse damper (16) through the first high-pressure plunger pump (2), an outlet of the pulse damper (16) is divided into two paths, one path is connected with a cold fluid inlet of the regenerator (17), and the other path is connected with a hot fluid outlet of the cooler (18).
6. The supercritical water circulating fluidized bed gasification system of claim 4, characterized by further comprising a second water tank (23), a cooling water pump (25) and a cooling tower (24); the second water tank (23) is connected with a cooling water inlet of the cooler (18) through a cooling water pump (25), a cooling water outlet of the cooler (18) is connected with an inlet of a cooling tower (24), and an outlet of the cooling tower (24) is connected with the second water tank (23).
7. The supercritical water circulating fluidized bed gasification system according to claim 1, wherein the gas extraction subsystem comprises a gas-liquid separator (21), a wet gas flowmeter (22) and a gas extraction bag, and the hot fluid outlet of the cooler (18) is connected with the inlet of the gas-liquid separator (21); the gas outlet of the gas-liquid separator (21) is divided into two paths, one path is connected with the wet gas flowmeter (22), and the other path is connected with the gas bag.
8. The supercritical water circulating fluidized bed gasification system of claim 1, further comprising a slag discharge subsystem, wherein the slag discharge subsystem comprises a first water tank (1), a slag discharge pump (5), a slag discharger (10) and a slag discharge cooler (11); the lower part of the lifting pipe (12) is provided with a slag discharge port, the first water tank (1) is connected with a water inlet of the slag discharge device (10) through a slag discharge pump (5), the slag discharge port of the lifting pipe (12) is connected with an inlet of the slag discharge cooler (11), an outlet of the slag discharge cooler (11) is connected with a waste slag inlet of the slag discharge device (10), and the bottom of the slag discharge device (10) is provided with a slag discharge port.
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| CN109988654A (en) * | 2019-04-29 | 2019-07-09 | 西安交通大学 | A kind of ciculation fluidized bed gasification system of supercritical water and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109988654A (en) * | 2019-04-29 | 2019-07-09 | 西安交通大学 | A kind of ciculation fluidized bed gasification system of supercritical water and method |
| CN109988654B (en) * | 2019-04-29 | 2024-07-16 | 西安交通大学 | Supercritical water circulating fluidized bed gasification system and method |
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