Continuous vaporization separation apparatus, system, and method using mixed gas hydrate method

Abstract

The application discloses a kind of mixed gas hydrate continuous vaporization separation device, system and method.The vaporization separation device includes ice breaking unit and vaporization unit, ice breaking unit and vaporization unit are communicated by several connecting channels;The bottom of the ice breaking unit is provided with hydrate slurry inlet, and a plurality of rotating shovels are arranged in the ice breaking unit from bottom to top, and each rotating shovel corresponds to a connecting channel port;The vaporization unit is sequentially provided with circulating cooling water outlet, backflushing water inlet, hydrate filter plate, tower plate, connecting channel interface, spraying water inlet and gas outlet from bottom to top.The device can realize continuous, stable hydrate vaporization decomposition and separation, ensure the integrity of hydrate production process, and ensure the smooth operation of process system.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of natural gas hydrate, and particularly relates to a mixed gas hydrate method continuous vaporization separation device, system and method. BACKGROUND

[0002] Natural gas hydrate is a kind of non-fixed crystal cage-shaped solid compound generated under high pressure and low temperature conditions, and is used to store and transport natural gas in the form of hydrate, and has the advantages of high efficiency, safety, energy saving, environmental protection and the like. 3 Natural gas hydrate can be decomposed into 164-180m 3 of natural gas, and according to this, it can be estimated that about 1.8x10 6 -2.1x10 6 m 3 of natural gas is contained in the global natural gas hydrate, which is equivalent to twice the total amount of carbon in the global proven conventional fossil fuels. Therefore, it is possible for natural gas hydrate to replace conventional fossil fuels in the future.

[0003] At present, it is found that when the amount of hydrate in the reactor is large, due to the four-phase equilibrium of hydrate-water-ice-gas in the system during the decomposition process, a decomposition buffer phenomenon occurs, which greatly reduces the overall decomposition rate of the hydrate. In addition, there are few studies on the continuous vaporization device and method of natural gas hydrate, and the main problem is to prevent the rapid and large release of gas during the vaporization process of natural gas hydrate, and the sudden increase in pressure and a large amount of natural gas affects the stability of the entire continuous production process. SUMMARY

[0004] In view of the problems of low vaporization efficiency of the existing hydrate method for separating mixed gas and difficult control of continuous vaporization process conditions, the present application provides a device and method which can be used for continuous vaporization separation of mixed gas by the hydrate method, realizes continuous and stable vaporization decomposition and separation after the mixed gas forms hydrate, ensures the integrity of the hydrate production process, and ensures the smooth operation of the process system.

[0005] According to a first aspect of the present application, the present application provides a hydrate continuous vaporization device.

[0006] Specifically, the hydrate continuous vaporization device comprises an ice breaking unit and a vaporization unit, and the ice breaking unit and the vaporization unit are communicated through a plurality of connecting channels;

[0007] The ice breaking unit is provided with a hydrate slurry inlet at the bottom, and a plurality of rotating shovel discs are arranged in the ice breaking unit from bottom to top, and each rotating shovel disc corresponds to a connecting channel port;

[0008] The circulation cooling water outlet, the backflush water inlet, the hydrate filter plate, the tray, the connecting channel interface, the spraying water inlet and the gas outlet are sequentially arranged in the vaporization unit from bottom to top.

[0009] Further, the ice breaking unit and the vaporization unit are both vertically arranged cylindrical structures.

[0010] Further, the connecting channel has a certain inclination angle, so that the ice breaking unit connecting channel interface is higher than the vaporization unit connecting channel interface. The inclination angle (i.e. the angle between the connecting channel and the horizontal plane) is generally 10°-60°, preferably 15°-45°. The connecting channel can be one or several, preferably two or more.

[0011] Further, the several connecting channels have different heights, i.e. the several connecting channels have openings or interfaces at different heights in the ice breaking unit and the vaporization unit, respectively.

[0012] Further, in the hydrate continuous vaporization device, the lower end of the outlet of the connecting channel in the vaporization unit is fixedly connected with the tray, and the inclination angle of the tray is the same as that of the connecting channel. The lower end (or the lower end) of the tray is provided with a notch as a dropping port, so that the slurry can flow onto the lower tray. Each connecting channel outlet is connected with a tray. Between the two adjacent connecting channel outlet trays, there is an opposite tray, the inclination direction of which is opposite to that of the adjacent tray, the high end of the tray is fixedly connected with the inner wall of the vaporization unit, and the low end of the tray is provided with a dropping port (notch) as a slurry flow channel.

[0013] Further, in the hydrate continuous vaporization device, the spraying water inlet is located at the upper part of the vaporization unit and is connected to the inside of the vaporization unit through a side water pipe. The spraying device can use a liquid distributor known in the art to achieve uniform spraying of the spraying water and ensure basic coverage of the tray cross section in the vaporization unit.

[0014] Further, in the hydrate continuous vaporization device, the rotating shovel disc is composed of rotating shafts and shovel discs. The rotating shafts are vertically perpendicular to the connecting channels, and the rotating shafts are arranged in parallel with each other. The shovel discs are semicircular concave and have folded edges. The folded edges of the shovel discs are of two types, one type is sawtooth-shaped and the other type is smooth structure. The shovel discs with different folded edges are alternately connected with the rotating shafts, the disc surfaces of the shovel discs are in the same plane as the rotating shafts, and the concave surfaces of the shovel discs are in the same direction. The top view of the shovel disc is semicircular, and the radius is equivalent to the inner diameter of the ice breaking unit.

[0015] Further, the ice breaking unit further comprises a driving device connected with the rotating shafts and used to drive the rotating shafts to rotate the shovel discs around the rotating shafts.

[0016] Further, in the hydrate continuous vaporization device, the hydrate filter plate is arranged at the bottom of the vaporization unit, generally at 1 / 5-1 / 4 of the vertical height of the bottom, and is oppositely inclined to the lowermost tray. That is, the filter plate is oppositely inclined to the lowermost tray. The filter structure on the hydrate filter plate is one or a combination of a filler structure, a wire mesh structure or a screen mesh structure, which is used to filter the hydrate slurry, so that the water produced after the decomposition of the hydrate and the spray water enter the bottom of the vaporization unit through the filter plate. The lower end of the filter plate is provided with a backflush water inlet, and a part of the filtered water can enter the filter plate in the vaporization unit through the backflush water inlet. The filtered water is opposite to the slurry flow direction, which prevents the slurry from accumulating on the filter plate and disperses the accumulated slurry at the bottom, thereby increasing the vaporization efficiency.

[0017] Further, in the hydrate continuous vaporization device, the circulating cooling water outlet is located at the bottom of the vaporization unit, and the liquid holdup of the vaporization unit is adjusted by a flow valve.

[0018] According to a second aspect of the present application, the present application provides a mixed gas hydrate continuous vaporization and separation system, which comprises the above-mentioned hydrate continuous vaporization device.

[0019] Specifically, the continuous vaporization and separation system comprises a mixed gas cooler, a hydrate reactor, a hydrate continuous vaporization device, a gas pump, a water pump and a solar water collecting tank. The mixed gas feed pipeline is connected with the mixed gas cooler, and then connected with the gas-liquid mixing nozzle on the feed inlet of the hydrate reactor. The hydrate slurry outlet of the hydrate reactor is connected with the slurry inlet of the hydrate continuous vaporization device through a pipeline. The circulating cooling water outlet of the hydrate continuous vaporization device is connected with the gas-liquid mixing nozzle on the feed inlet of the hydrate reactor and the water inlet of the solar water collecting tank, respectively. The spray water inlet of the hydrate continuous vaporization device is connected with the water outlet of the solar water collecting tank through the water pump.

[0020] Further, the gas pump is connected with the gas outlet of the vaporization unit, and the water pump is connected with the spray water inlet of the solar water collecting tank and the vaporization unit.

[0021] Further, in the vaporization and separation system, the hydrate reactor is provided with a first gas outlet at the top, and is provided with a gas-liquid mixing nozzle, a contact baffle and a hydrate reaction tray from top to bottom inside the reactor, and is provided with a hydrate slurry outlet at the bottom. The hydrate reactor is provided with a back pressure valve.

[0022] Further, the back pressure valve is set to a pressure of 0.5-8 MPa.

[0023] Further, in the vaporization separation system, the outlet of the circulating cooling water of the continuous vaporization device is located at the bottom of the vaporization unit, and is connected to the liquid inlet of the gas-liquid mixing nozzle through a three-way pipe.

[0024] Further, in the vaporization separation system, the spray water inlet of the continuous vaporization device is located at the top of the vaporization unit, and is connected to the inside of the vaporization unit through a side water pipe. The spray device can use a liquid distributor known in the art, which can realize uniform spraying of the spray water and ensure that the vaporization unit is basically covered.

[0025] Further, the gas outlet has a gas pump to extract gas, and a three-way pipe and a flow control valve are used to inject a certain volume of gas into the bottom of the hydrate reactor to increase the reaction pressure and promote the reaction balance.

[0026] Further, in the vaporization system, the rotation directions of the adjacent two groups of rotating shovels in the ice breaking unit are the same, and when one of the shovels in the upper group of rotating shovels is operated to the vertical direction and points downward to the rotating shaft of the adjacent rotating shovel in the lower group, the position should coincide with the midline of the two adjacent shovels in the lower group of rotating shovels. The ratio of the distance between the two groups of rotating shafts to the radius of the shovel is 1.732~2.828:1, so as to ensure that the two groups of rotating shovels will not collide mechanically. The rotation speeds of the two shovels are the same, and the angular velocity is 0.08 rad / s~0.2 rad / s. As the amount of hydrate in the lower group increases, the amount of hydrate carried by the lowermost shovel will increase, and when it is rotated to the uppermost position, a part of the slurry will be carried away by the adjacent upper group of shovels, which will play a role in breaking the whole into parts and preventing the hydrate from self-sealing and caking. At the same time, the vaporization efficiency of a small amount of slurry is higher.

[0027] Further, in the vaporization separation system, the solar heat collecting water tank is a closed water storage tank, and a solar heat collecting plate is laid on the top of the tank for heating the water in the tank by solar energy. The heating temperature is 10℃~25℃.

[0028] According to a third aspect of the present application, the present application provides a mixed gas hydrate continuous vaporization separation method, wherein the mixed gas hydrate continuous separation system described above is applied.

[0029] Specifically, a mixed gas hydrate continuous vaporization separation method comprises the following contents:

[0030] (1) The mixed gas is pre-cooled by a heat exchanger, and the temperature is T0; after pre-cooling, the mixed gas is pressurized together with the circulating cooling water, and is injected into the hydrate reactor through a gas-liquid mixing nozzle; the hydrate reaction is carried out in the hydrate reactor through a contact baffle and a hydrate reaction tray respectively; the reaction pressure in the hydrate reactor is set as P1, and the temperature is T1;

[0031] (2) The water in the solar energy collection tank is preheated to a temperature T2, and the water in the solar energy collection tank is pumped into the gasification unit of the continuous gasification device by opening the water pump;

[0032] (3) The mixed gas reacts with water on the hydrate reaction tower plate and the hydrate promoter on the polymer gel material to produce hydrates. The slurry flows into the bottom and flows out through the hydrate slurry outlet, and enters the continuous gasification device. The gas that does not form hydrates is discharged through the first gas outlet;

[0033] (4) After the hydrate slurry enters the continuous gasification device, it is accumulated in the icebreaking unit and is turned upward under the action of the two rotating shovels and enters the connecting channel under the action of gravity. The hydrate slurry is heated on the inclined tower plate under the action of the spray water in the gasification unit, and the gasification gas is extracted by opening the gas pump. After the separated gas is extracted, the pressure in the gasification unit is reduced, which promotes the decomposition of the hydrate;

[0034] (5) The water and the un-decomposed hydrates in the gasification unit are filtered on the hydrate filter plate. The water enters the cooling water circulation pipeline from the bottom, a part of the water enters the hydrate reactor to continue to participate in the water and reaction, a part of the water enters the solar energy collection tank for heating and circulation, and a part of the water enters the gasification unit to reverse wash the filter plate to prevent the un-decomposed slurry from accumulating on the filter plate.

[0035] Further, in the above-mentioned continuous gasification separation method, the pre-cooling temperature T0 is -20~0℃.

[0036] Further, in the above-mentioned continuous gasification separation method, the operating conditions of the hydrate reactor are: the pressure P1 is 0.1MPa~8.0MPa, and the temperature T1 is -10~15℃. The specific operating conditions need to be determined according to the mixed gas system to be treated and the type of additive selected.

[0037] Further, in the above-mentioned continuous gasification separation method, the hydrate reaction in step (1) can be a reaction of gas and aqueous solution, or various thermodynamic and kinetic promoters can be added, such as one or more of sodium dodecyl sulfate (SDS), sodium dodecyl benzene sulfonate (SDBS), linear alkyl sulfonate sodium (LAB-SA), alkyl polyglycoside (APG), tetrahydrofuran (THF), tetrabutylammonium bromide (TBAB), cyclopentane (CP) and acetone.

[0038] Further, in the above-mentioned continuous gasification separation method, the water temperature T2 preheated by the solar energy collection tank in step (2) is 20℃~50℃.

[0039] Further, in the continuous vaporization separation method, the hydrate slurry in step (3) refers to a mixture of hydrates and liquid that has not reacted to form hydrates, and the volume ratio of reaction control hydrates in the hydrate slurry is 30% to 80%, preferably 50% to 70%.

[0040] Further, in the continuous vaporization separation method, the operating conditions of the hydrate continuous vaporization device in step (4) are: the ice breaking unit pressure is 0.05 MPa to 3.0 MPa, the ice breaking unit temperature is -5°C to 10°C, the vaporization unit pressure is 0.05 MPa to 1.0 MPa, and the ice breaking unit temperature is 10 to 50°C.

[0041] Further, in the continuous vaporization separation method, the rotating speed of the rotating shovel disc of the ice breaking unit in step (4) is preferably 100 r / min to 300 r / min.

[0042] Further, in the continuous vaporization separation method, the circulating volume ratio of water in the cooling water circulating pipeline in step (5) is 5% to 55%.

[0043] In the present application, "up" and "down" are used for description purposes only and should not be understood as indicating or implying relative importance. The technical term "several" refers to two or more, unless otherwise explicitly limited.

[0044] Compared with the prior art, the present application has the following advantages:

[0045] 1. The continuous vaporization device is used, which has the characteristics of breaking the hydrates into small pieces by the rotating shovel disc and vaporizing them in multiple connection channels. The hydrates are first broken and turned over by the sawtooth shovel disc in the ice breaking unit, then loaded by the spoon-shaped shovel disc and brought into the connection channel. The continuous breaking and turning over can slowly destroy the self-sealing effect of the hydrates, form micro-cracks on the surface of the hydrates, and the rotation of the shovel disc can bring the hydrates into the connection channel for vaporization in the vaporization unit, which stabilizes the pressure of the vaporization system.

[0046] 2. The vaporization unit in the continuous vaporization device uses inclined trays and water spraying, the hydrate slurry is vaporized by flowing on the trays and heat exchange with warm water, and the heat exchanged water can be recycled, reducing the investment and energy consumption of heating facilities, and the energy saving effect is obvious.

[0047] 3. The vaporization unit of the continuous vaporization device adopts the structure of the inclined filter plate and the backflushing water. Firstly, the inclined direction of the filter plate is opposite to the last tray, which can prevent the slurry flowing down from the tray from piling up on one side of the filter plate; secondly, the backflushing water inlet is arranged on the lower side of the filter plate, the backflushing water is opposite to the direction of the slurry flowing down, and the backflushing water disperses the slurry to prevent the self-sealing effect; thirdly, the force of the backflushing water can realize the flushing effect of the filter plate. BRIEF DESCRIPTION OF DRAWINGS

[0048] Figure 1 Figure 1 is a schematic diagram of the continuous vaporization separation device of the present application.

[0049] In the figure, the marks are as follows: 1-ice breaking unit, 2-vaporization unit, 3-hydrate slurry inlet, 4-rotary shovel disc, 5-connection channel, 6-gas outlet, 7-spraying water inlet, 8-tray, 9-hydrate filter plate, 10-circulating cooling water outlet, 11-backflushing water inlet.

[0050] Figure 2 Figure 2 is a schematic diagram of the mixed gas continuous vaporization separation system of the present application.

[0051] In the figure, the marks are as follows: 21-mixed gas feeding pipeline, 22-mixed gas cooler, 23-gas-liquid mixed nozzle, 24-hydrate reactor, 25-first gas discharge pipeline, 26-hydrate slurry pipeline, 27-hydrate continuous vaporization device, 28-gas pump, 29-second gas discharge pipeline, 30-gas backflow pipeline, 31-circulating water discharge pipeline, 32-circulating water backflow pipeline, 33-circulating water recirculation pipeline, 34-solar water collecting tank, 35-solar water collecting plate, 36-water pump, 37-spraying water inlet pipeline, 38-backflushing water pipeline, 201-first gas valve, 202-hydrate slurry discharge valve, 203-second gas valve, 204-gas backflow valve, 205-circulating water valve, 206-circulating water backflow valve, 207-circulating water recirculation valve, 208-backflushing water valve. DETAILED DESCRIPTION

[0052] The specific embodiments of the present application will be further described in detail below with reference to the accompanying drawings. The following examples are used to illustrate the present application, but are not used to limit the scope of the present application.

[0053] As Figure 1As shown, the continuous vaporization device for hydrates of the present invention includes an ice-breaking unit 1 and a vaporization unit 2, both of which are vertical cylindrical structures. The ice-breaking unit 1 and the vaporization unit 2 are connected by connecting channels 5, and in this embodiment, two connecting channels 5 are used as an example. The bottom of the ice-breaking unit 1 is provided with a hydrate slurry inlet 3, and the interior is provided with rotating shovels 4 from bottom to top, and in this embodiment, two rotating shovels are used as an example. Each channel opening in the vaporization unit should be provided with a rotating shovel 4. The vaporization unit 2 is provided with a circulating cooling water outlet 10, a hydrate filter plate 9, a tower plate 8, a spray water inlet 7, and a gas outlet 6 from bottom to top. The spray water inlet 7 is connected to a nozzle through a pipeline, with the nozzle located at the center of the top of the vaporizer. The hydrate filter plate 9 is located below the tower plate 8.

[0054] The inclination angle of the connecting channel 5 is 20°. The rotating shovel 4 has four shovels, two of which are serrated and two are smooth, and they are alternately connected to the rotating shaft.

[0055] like Figure 2 As shown, the vaporization separation system of the present invention includes a mixed gas cooler 22, a hydrate reactor 24, a hydrate continuous vaporization device 27, a gas pump 28, a water pump 36, and a solar water collection tank 34. The mixed gas cooler 22 is connected to the mixed gas feed line 21, and then to the gas-liquid mixing nozzle 23 on the feed inlet of the hydrate reactor 24; the hydrate slurry outlet of the hydrate reactor 24 is connected to the slurry inlet of the hydrate continuous vaporization device 27 via the hydrate slurry line 26; the circulating water discharge line 31 of the hydrate continuous vaporization device 27 is located at the bottom and is connected to the circulating water return line 32 and the circulating water recirculation line 33 respectively; the circulating water return line 32 is connected to the gas-liquid mixing nozzle 23 on the hydrate reactor 24; the circulating water recirculation line 33 is connected to the inlet of the solar heat collection tank 34; the spray water inlet line 37 of the hydrate continuous vaporization device 27 is connected to the outlet of the solar heat collection tank 34 via the water pump 36; the solar heat collection tank 34 is equipped with a solar collector plate 35.

[0056] Combination Figures 1-2The process of treating the mixed gas by the mixed gas continuous vaporization separation system of the present application is as follows: the mixed gas enters the mixed gas cooler 22 through the mixed gas feeding pipeline 21 to be cooled and exchanged, then enters the gas-liquid mixing nozzle 23, the liquid is fed into the gas-liquid mixing nozzle 23 by the circulating water return pipeline 32, and the gas-liquid mixture enters the hydrate reactor 24. The gas-liquid mixture is reacted in the hydrate reactor 24, the gas not forming hydrate is discharged through the first gas discharge pipeline 25, the hydrate slurry is discharged from the hydrate slurry pipeline 26 and enters the hydrate continuous vaporization device 27 to be continuously vaporized for a plurality of times, the vaporized gas is extracted by the gas pump 28, part of the gas is injected into the hydrate reactor 24 through the gas return pipeline 30 to maintain the pressure and promote the reaction equilibrium movement, and the remaining gas is discharged through the second gas discharge pipeline 29; the water in the solar water collecting tank 34 is heated by the solar heat collecting plate 35, is pressurized by the water pump 36, enters the spraying water inlet pipeline 37, and is sprayed on the nozzle in the hydrate continuous vaporization device 27; the spraying water enters the circulating water discharge pipeline 31 through the hydrate filter plate of the hydrate continuous vaporization device 27, part of the circulating water enters the hydrate reactor 24 through the circulating water return pipeline 32 to continue the hydrate reaction, and part of the circulating water enters the solar water collecting tank 34 through the circulating water recirculation pipeline 33 to be reheated.

[0057] Example 1

[0058] The hydrate continuous vaporization device provided by the present application is used to treat the mixed gas Figure 2The shown process is for hydrate separation of a mixture of CO2 and CH4, which contains 85% CH4 and the rest is N2 and O2. The mixture is pre-cooled in a mixture cooler 22 at -10°C. The pre-cooled mixture is pressurized to 3 MPa with circulating cooling water and sprayed into a hydrate reactor 24 through a gas-liquid mixing nozzle 23. The reaction conditions in the hydrate reactor 24 are 3 MPa and 0°C. The gas-liquid mixture collides with a baffle in the hydrate reactor 24 and then reacts on the tower plates 8 coated with silicone adhesive, polyurethane sponge layer, poly N-isopropylamide gel and tetra-butyl ammonium bromide hydrate promoter from top to bottom. The sponge layer is 0.6 cm thick, the water content of the polymeric gel material is 85%, and the hydrate promoter concentration is 5 wt% solution. The volume ratio of the generated hydrate in the hydrate slurry is 60%, the water temperature in the solar water collector 34 is 30°C, the water pump 36 is opened, and the water in the solar water collector 34 is pumped into the vaporization unit 2 of the hydrate continuous vaporization device 27. The hydrate slurry discharge valve 202 is opened, the slurry is discharged through the hydrate slurry pipeline 26 and enters the hydrate continuous vaporization device 27. The gases N2 and O2 that do not form hydrates are discharged through the first gas valve 201. The hydrate slurry enters the continuous vaporization device 27 and accumulates in the ice-breaking unit 1, which has a pressure of 2.0 MPa and a temperature of 0°C. The stirring speed of the stirring paddle is 100 r / min. The hydrate is turned upward under the action of the rotating shovel, the upper shovel brings the hydrate slurry in the lower shovel into the connecting channel 5 and enters the vaporization unit 2 under the action of gravity. The pressure in the vaporization unit 2 is 1.0 MPa and the temperature is 20°C. The hydrate slurry is heated on the inclined tower plate 8 under the action of the spray water, and the gas pump 28 is opened. After the vaporized gas is extracted, the pressure in the vaporization unit 2 is reduced, which promotes the decomposition of the hydrate. The water and the incomplete decomposition of the hydrate in the vaporization unit 2 are filtered on the hydrate filter plate 9, the circulating water backflow valve 206 is opened, 30% of the backflow water enters the circulating water backflow pipeline 32 and enters the hydrate reactor 24 again to continue to participate in the water reaction, and the remaining 70% of the circulating water enters the solar water collector 34 through the circulating water recirculation pipeline 33 for heating and circulation.

[0059] Comparative Example 1

[0060] The same as example 1, except that the hydrate vaporization device adopts a conventional single tower form, and the whole hydrate and its slurry (60% hydrate content) is heated to realize the vaporization of the hydrate. Compared with example 1, due to the internal heat transfer of the hydrate after contacting the heat source, the hydrate forms a self-sealing effect at a suitable internal temperature, which greatly increases the energy consumption and vaporization time, and increases the operation cost. In addition, due to the whole heating, the pressure in the hydrate vaporization device is unstable, which increases the operation risk.

Claims

1. A hydrate continuous vaporization apparatus characterized by, The ice-breaking unit and the vaporization unit are communicated through several connecting channels; the ice-breaking unit is provided with a hydrate slurry inlet at the bottom, and several rotating scoops are arranged in the ice-breaking unit from bottom to top, each rotating scoop corresponding to a connecting channel opening; the vaporization unit is sequentially provided with a circulating cooling water outlet, a backflushing water inlet, a hydrate filter plate, a tower plate, a connecting channel interface, a spraying water inlet and a gas outlet from bottom to top; The rotating scoop is composed of a rotating shaft and a scoop; the rotating shaft is radially perpendicular to the connecting channel, and each rotating shaft is arranged in parallel with each other; the scoop is in a semicircular concave shape with a folded edge.

2. The vaporization device of claim 1, wherein The ice-breaking unit and the vaporization unit are both vertically arranged in a cylindrical structure.

3. The vaporization device of claim 1, wherein The connecting channel has a certain inclination angle, so that the ice-breaking unit connecting channel interface is higher than the vaporization unit connecting channel interface.

4. The vaporization device of claim 3, wherein The inclination angle is 10°-60°.

5. The vaporization device of claim 1, wherein The several connecting channels have openings or interfaces at different heights of the ice-breaking unit and the vaporization unit.

6. The vaporization device of claim 1, wherein The tower plate in the vaporization unit is fixedly connected with the lower edge of the outlet of the connecting channel, and the inclination angle of the tower plate is the same as that of the connecting channel; the lower end of the tower plate is provided with a notch as a material dropping port.

7. The vaporization device of claim 6, wherein Each connecting channel outlet is connected with a tower plate, and an opposite tower plate is arranged between the two adjacent connecting channel outlet tower plates, the inclination direction of the opposite tower plate is opposite to that of the adjacent tower plate, the high end of the opposite tower plate is fixedly connected with the inner wall of the vaporization unit, and the low end of the opposite tower plate is provided with a material dropping port.

8. The vaporization device of claim 1, wherein The spraying water inlet is located at the upper part of the vaporization unit and is connected with the inside of the vaporization unit through a side water pipe.

9. The vaporization device of claim 1, wherein The folded edge includes two structures, namely, a sawtooth structure and a smooth structure; the two kinds of scoops are alternately connected with the rotating shaft in sequence, the scoop surface is in the same plane as the rotating shaft, and the concave surfaces of the scoops are in the same direction.

10. The vaporization device of claim 1, wherein The ice-breaking unit further comprises a driving device connected with the rotating shaft and used for driving the rotating shaft to rotate the scoop around the rotating shaft.

11. The vaporization device of claim 1, wherein The hydrate filter plate is arranged at the bottom of the vaporization unit and is arranged in an opposite inclination with the lowermost tower plate.

12. The vaporization device of claim 11, wherein The lower end of the filter plate is provided with a backflushing water inlet.

13. A continuous vaporization and separation system for mixed gas hydrate, comprising the hydrate continuous vaporization device according to any one of claims 1-11.

14. The separation system of claim 13, wherein, The continuous vaporization and separation system comprises a mixed gas cooler, a hydrate reactor, a hydrate continuous vaporization device, a gas pump, a water pump and a solar water collecting tank; a mixed gas feeding pipeline is connected with the mixed gas cooler, and then connected with a gas-liquid mixing nozzle on the feeding port of the hydrate reactor; a hydrate slurry outlet of the hydrate reactor is connected with a slurry inlet of the hydrate continuous vaporization device through a pipeline; a circulating cooling water outlet of the hydrate continuous vaporization device is connected with the gas-liquid mixing nozzle on the feeding port of the hydrate reactor, and a water inlet of the solar water collecting tank; a spraying water inlet of the hydrate continuous vaporization device is connected with a water outlet of the solar water collecting tank through a water pump.

15. The separation system of claim 14, wherein, The gas pump is connected with the gas outlet of the vaporization unit; the water pump is connected with the spraying water inlet of the vaporization unit and the solar water collecting tank.

16. The separation system of claim 14, wherein The hydrate reactor is provided with a first gas outlet at the top, gas-liquid mixing nozzles, contact baffles and hydrate reaction trays from top to bottom inside the reactor, and a hydrate slurry outlet at the bottom.

17. The separation system of claim 14, wherein The circulating cooling water outlet of the continuous vaporization device is located at the bottom of the vaporization unit and is connected to the liquid inlet of the gas-liquid mixing nozzle through a three-way valve.

18. The separation system of claim 14, wherein, When one of the upper group of rotating shovels is operated to the vertical direction and points downward to the rotating shaft of the adjacent lower rotating shovel, the position should coincide with the midline of the two adjacent shovels in the lower group of rotating shovels.

19. A continuous vaporization and separation method of mixed gas hydrate method, wherein the continuous vaporization and separation system of mixed gas hydrate method of any one of claims 13-18 is applied.

20. The continuous vaporization separation process according to claim 19, characterized in that, The method comprises the following steps: (1) The mixed gas is pre-cooled by a heat exchanger to a temperature of T0, and then pressurized together with the circulating cooling water, and sprayed into the hydrate reactor through the gas-liquid mixing nozzle; the hydrate reaction is carried out in the hydrate reactor through the contact baffles and the hydrate reaction trays; the reaction pressure in the hydrate reactor is set to P1, and the temperature is T1; (2) The water in the solar heat collection tank is preheated to a temperature of T2, and the water pump is opened to pump the water in the solar heat collection tank into the vaporization unit of the continuous vaporization device; (3) The mixed gas reacts with the water on the polymer gel material and the hydrate promoter on the hydrate reaction tray to form hydrates, and the hydrate slurry flows into the bottom and flows out through the hydrate slurry outlet, and enters the continuous vaporization device; the gas that does not form hydrates is discharged through the first gas outlet; (4) The hydrate slurry enters the ice-breaking unit, is turned upward under the action of the two rotating shovels, enters the connecting channel, and enters the vaporization unit under the action of gravity; the hydrate slurry in the vaporization unit is first heated on the inclined tray under the action of the spray water, and the gas is extracted by opening the gas pump; after the separated gas is extracted, the pressure in the vaporization unit is reduced, promoting the decomposition of the hydrates; (5) The water and the un-decomposed hydrates in the vaporization unit are filtered on the hydrate filter plate, and the water enters the cooling water circulation pipeline from the bottom, part of the water enters the hydrate reactor to continue to participate in the water and reaction, part of the water enters the solar heat collection tank for heating and circulation, and part of the water enters the vaporization unit to reverse wash the filter plate through the backflush valve to prevent the un-decomposed slurry from accumulating on the filter plate.

21. The continuous vaporization separation process according to claim 20, characterized in that, T0 is -20~0℃.

22. The continuous vaporization and separation method according to claim 20, wherein the operating conditions of the hydrate reactor are: the pressure P1 is 0.1MPa~8.0MPa, and the temperature T1 is -10~15℃.

23. The continuous vaporization separation process according to claim 20, characterized in that, T2 is 20℃~50℃.

24. The continuous vaporization separation process according to claim 20, characterized in that, The hydrate slurry in step (3) refers to a mixture of formed hydrates and unreacted hydrate-forming liquid, and the volume ratio of the reaction control hydrate in the hydrate slurry is 30%~80%.

25. The continuous vaporization separation process according to claim 20, characterized in that, The operation conditions of the hydrate continuous vaporization device in step (4) are as follows: the ice-breaking unit pressure is 0.05 MPa-3.0 MPa, the ice-breaking unit temperature is-5 ℃-10 ℃, the vaporization unit pressure is 0.05 MPa-1.0 MPa, and the ice-breaking unit temperature is 10-50 ℃.

26. The continuous vaporization separation process according to claim 20, wherein The circulating volume ratio of water in the cooling water circulating pipeline in step (5) is 5%-55%.

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