CN110577851A - device and method for quickly and continuously hydrating and separating coal bed gas - Google Patents
device and method for quickly and continuously hydrating and separating coal bed gas Download PDFInfo
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- CN110577851A CN110577851A CN201910865198.2A CN201910865198A CN110577851A CN 110577851 A CN110577851 A CN 110577851A CN 201910865198 A CN201910865198 A CN 201910865198A CN 110577851 A CN110577851 A CN 110577851A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/105—Removal of contaminants of nitrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/108—Production of gas hydrates
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Abstract
A device and a method for quickly and continuously hydrating and separating coal bed gas. The device mainly comprises a feeding gas circuit, a separation liquid circulation circuit, a hydration separation tower, a nitrogen-rich gas circuit, a methane-rich gas circuit, a connecting pipeline and a valve. And the feeding gas path is connected with a gas cylinder, a gas pressure reducing valve, a gas buffer tank, a pressurization system and a first gas flowmeter. The method is characterized in that nitrogen is difficult to dissolve in an oil phase, methane is easy to dissolve in the oil phase, water-in-oil emulsion is used as a separation liquid, the contact area of the methane and water is increased, the separation liquid flows down along a spiral channel in a tiled film shape under the action of a liquid inlet distributor at the upper part of a separation tower, mixed gas is introduced from the bottom of the tower and contacts with the separation liquid in a countercurrent mode along the spiral channel, and hydrate is rapidly generated and flows to the bottom of the tower in a hydrate slurry mode. The invention has the advantages of increasing the gas-liquid contact area, strengthening mass transfer, quickly generating hydrate, ensuring the mobility of hydrate slurry and improving the separation selectivity by adopting the water-in-oil emulsion.
Description
Technical Field
The invention relates to the field of separation and purification of mixed gas, in particular to a device and a method for quickly and continuously hydrating and separating coal bed gas.
Technical Field
coal bed methane, also known as Coal Bed Methane (CBM), is widely produced and stored in coal seams. China has abundant coal bed gas resources within the depth range of 2000 m underground, and the total amount is 31 multiplied by 1012 m3. The coal mining in China mainly adopts underground extraction, the pressure of the extracted coal bed gas is low, and the CH content in 2/3 coal bed gas4The volume fraction is lower than 30 percent, and the air is mixed with the air, most of the air is directly discharged into the atmosphere, and the discharge amount reaches 1.9 multiplied by 10 every year10 m3Equivalent to 2.0X 108the standard coal not only causes energy waste, but also pollutes the environment and destroys the climate.
The main methods for separating the mixed gas at present are as follows: cryogenic process, pressure swing adsorption process, membrane separation process. The three methods are widely applied in industry and mature in technology, but have some inherent limitations. The cryogenic separation method can be realized only by cascade refrigeration, has high energy consumption, more complex circulating refrigeration process, large device investment, strict requirements on the content of impurities in raw materials and generally low product purity. The pressure swing adsorption technology uses a plurality of devices, occupies a large area, has complex process and program control, needs frequent switching and has large equipment investment. The membrane separation method has the advantages of low recovery rate and product purity, high requirements on membrane materials, short service life of the membrane, high cost and easy loss of gas, and is only suitable for small-scale mixed gas purification devices.
The hydrate separation mixed gas method is a new separation technology in recent years, a water-in-oil emulsion is used as a separation medium, and the coal bed gas is subjected to absorption and hydration twice separation by utilizing the characteristic that hydrocarbons are easily dissolved in an oil phase, so that the separation selectivity of methane can be improved. Compared with the traditional separation method, the hydrate method has the advantages of small pressure loss, low cost, mild reaction conditions, simple and safe process, easy industrial continuous production and the like.
Although many studies have been made and great progress has been made in recent years for separating various mixed gases by using hydrates, the separation is basically performed intermittently, the continuity is poor, the production efficiency is low, and the industrialization is difficult to realize.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provides a device and a method for hydration and separation of coal bed gas with high selectivity, low energy consumption and high speed and continuity.
the purpose of the invention is realized by the following technical scheme:
A device for quickly and continuously hydrating and separating coal bed gas comprises a feeding gas circuit, a separation liquid circulation circuit, a hydration separation tower, a nitrogen-rich gas circuit and a methane-rich gas circuit; the hydration separation tower is provided with an air inlet, a liquid inlet, a nitrogen-rich gas outlet, a hydrate slurry outlet, a cooling liquid inlet and a cooling liquid outlet; the feeding gas circuit comprises a gas cylinder, a gas pressure reducing valve, a gas buffer tank, a pressurization system, a first gas flowmeter, a first stop valve, a first emptying valve, a second stop valve and a third stop valve; the gas cylinder, the gas pressure reducing valve, the gas buffer tank, the pressurization system and the first gas flowmeter are sequentially connected through a pipeline, and the first gas flowmeter is connected with a gas inlet of the hydration separation tower through a pipeline; a first stop valve is arranged between the gas pressure reducing valve and the gas buffer tank, the top of the gas buffer tank is connected with a first emptying valve through a tee joint, a second stop valve is arranged between the gas buffer tank and the pressurization system, and a third stop valve is arranged between the first gas flowmeter and the hydration separation tower; the feeding gas circuit is connected to a gas inlet of the hydration separation tower through a pipeline; the separation liquid circulating loop comprises a separation liquid storage tank, a first liquid level monitoring device, a liquid delivery pump, a liquid flow meter, a second liquid level monitoring device, a solid-liquid mixed delivery pump, a decomposer, a third liquid level monitoring device, a first electromagnetic valve, a second electromagnetic valve, a third electromagnetic valve, a second emptying valve, a second liquid discharge port, a charging port, a third liquid discharge port and a fourth stop valve; a liquid inlet of the hydration separation tower is sequentially connected with a liquid flowmeter and a liquid delivery pump, and the liquid delivery pump is connected with the bottom end of a separation liquid storage tank; a hydrate slurry outlet of the hydration separation tower is sequentially connected with a solid-liquid mixed transportation pump, a decomposer and a separation liquid storage tank; the first electromagnetic valve is positioned on a pipeline between the hydration separation tower and the solid-liquid mixed transportation pump and is used for controlling the liquid level of the bottom in the hydration separation tower in cooperation with the second liquid level monitoring device and the solid-liquid mixed transportation pump; the second electromagnetic valve is positioned on a pipeline between the decomposer and the separation liquid storage tank and is used for controlling the liquid level of the bottom in the decomposer in a cooperative manner with the third liquid level monitoring device; the third electromagnetic valve is positioned on a pipeline between the separation liquid storage tank and the liquid delivery pump and is used for controlling the liquid level in the separation liquid storage tank in cooperation with the first liquid level monitoring device and the liquid delivery pump; the second emptying valve is positioned on a right end pipeline of the tee joint at the top of the decomposer and is used for emptying residual gas in the decomposer when the operation is finished; the second liquid outlet is positioned on a right end pipeline of the tee joint at the bottom of the decomposer and is used for discharging residual liquid in the decomposer when the operation is finished; the feed inlet is positioned at the top of the separation liquid storage tank and is used for adding the separation liquid into the separation liquid storage tank; the third liquid outlet is positioned on a right end pipeline of the tee joint at the bottom of the separation liquid storage tank and is used for discharging residual liquid in the separation liquid storage tank when the operation is finished; the fourth stop valve is positioned on a pipeline between the liquid flowmeter and the liquid inlet; the first liquid level monitoring device is positioned on the liquid level in the separation liquid storage tank and controls the switch of the third electromagnetic valve and the liquid delivery pump through current signals; the second liquid level monitoring device is positioned on the liquid level at the bottom in the hydration separation tower, and controls the switch of the first electromagnetic valve and the solid-liquid mixed transportation pump through current signals; the third liquid level monitoring device is positioned on the liquid level in the decomposer and controls the switch of the second electromagnetic valve through a current signal;
The separation liquid circulation loop is connected to a liquid inlet of the hydration separation tower through a pipeline, hydrate slurry generated by hydration reaction in the separation tower is conveyed into the decomposer from a hydrate slurry outlet at the bottom through the solid-liquid mixed conveying pump, and the separation liquid flows into the separation liquid storage tank by gravity after the hydrate is decomposed, and then is conveyed into the separation tower through the liquid conveying pump for recycling;
The nitrogen-rich gas path is connected with a back pressure valve, a second gas dryer and a third gas flowmeter, and a nitrogen-rich gas outlet of the hydration separation tower is connected with the back pressure valve, the second gas dryer and the third gas flowmeter in sequence;
the methane-rich gas path is connected with a one-way check valve, a first gas drier and a second gas flowmeter, hydrate slurry generated in the separation tower is pumped into the decomposer through a hydrate slurry outlet, and an outlet at the top of the decomposer is sequentially connected with the one-way check valve, the first gas drier and the second gas flowmeter; and the methane-rich gas generated by decomposing the hydrate in the decomposer is discharged from the top, enters the methane-rich gas circuit and is then discharged from a methane-rich gas outlet.
Furthermore, the buffer tank is provided with a cooling jacket for precooling the raw material gas, so that the stability of the hydration reaction condition in the hydrate separation tower is improved, the buffer tank is connected with a thermometer and a pressure gauge for monitoring the temperature and the pressure of the raw material gas in the buffer tank, and the top of the buffer tank is also connected with a first emptying valve which can resist the pressure of 20 MPa.
Further, the temperature and pressure condition in the hydrate separation tower is monitored by a temperature and pressure monitoring system, and the hydrate separation tower is further provided with an emptying valve, a liquid outlet and a window.
furthermore, the hydration separation tower is a cylindrical tower reactor with the height-diameter ratio of 4 ~ 8:1, the pressure resistance of the hydration separation tower is 15MPa, the interior of the hydration separation tower is of a spiral channel structure, the channel is seamlessly welded with the support and the inner wall of the separation tower, a hydrophobic nano coating is coated on the channel, water-in-oil emulsion can flow down on the channel in a form of a flat film, hydrate cannot be adhered on the channel, the hydration separation tower is connected with a temperature and pressure monitoring system, cooling liquid is introduced into a cooling jacket of the separation tower and the inner support to control the temperature in the hydration tower to be 273 ~ 276K, and the tower is also provided with a vent valve, a liquid discharge port and a.
furthermore, a box-shaped uniform distributor is arranged on a spiral channel at the liquid inlet position, a liquid inlet pipe opening is wrapped in the spiral channel, interfaces at the edge of the uniform distributor are welded in a seamless mode, an upstream baffle of the uniform distributor is a solid stainless steel plate, a downstream baffle of the uniform distributor is a stainless steel plate with a plurality of grid-type small channels arranged on the lower edge, the width of a grid hole is 1 mm ~ 5 mm, the height of the grid hole is 1 ~ 3 mm, and the separation liquid is uniformly distributed.
furthermore, a first liquid level monitoring device, a second liquid level monitoring device and a third liquid level monitoring device are connected to the separation liquid circulation loop, the liquid level monitoring devices control the electromagnetic valve and the liquid delivery pump/solid-liquid mixed delivery pump to be switched on and off, once the liquid level is monitored to be lower than a set value, the liquid level control system gives a current signal to the electromagnetic valve and the delivery pump, the electromagnetic valve and the pump are switched off, and the electromagnetic valve and the delivery pump are switched on after the liquid level is restored, so that the effect of maintaining the stability and the safe operation of the system is achieved.
Further, the decomposer is arranged at a position higher than the separation liquid storage tank, so that the separation liquid at the bottom of the decomposer flows into the separation liquid storage tank under the action of gravity. The decomposer is a hydrate decomposition reactor with a heating jacket, a thermometer is connected to monitor the internal temperature, the pressure resistance is 15MPa, gas is discharged from a top one-way check valve after hydrate slurry is decomposed in the hydrate decomposition reactor, separation liquid flows into a separation liquid storage tank from a bottom electromagnetic valve, and the hydrate decomposition reactor is provided with a third liquid level monitoring device, an emptying valve and a liquid outlet. The separation liquid storage tank is provided with a cooling jacket, can pre-cool the separation liquid, improves the stability of the hydration reaction condition in the separation tower, and is connected with a thermometer and a first liquid level monitoring device which is provided with a feed inlet and a liquid outlet.
Furthermore, the continuous feeding and discharging can be realized, the separation liquid can be recycled, the flow of the separation liquid is detected and recorded by a liquid flowmeter, the flow of the raw material gas is detected and recorded by a first gas flowmeter, and the nitrogen-rich gas and the methane-rich gas are respectively dehydrated by a second gas dryer and the first gas dryer and then detected, recorded and calculated by a third gas flowmeter and a second gas flowmeter arranged on the pipeline to obtain the gas yield. The nitrogen-rich pipeline is also connected with a back pressure valve for maintaining the pressure condition of the gas in the separation tower.
A method for quickly and continuously hydrating and separating coal bed gas utilizes the characteristic that nitrogen is difficult to dissolve in an oil phase and methane is easy to dissolve in the oil phase, adopts water-in-oil emulsion as a separation liquid to dissolve methane in the oil phase, then the methane is contacted and dissolved with small water beads distributed in the oil phase, the contact area of the methane and water is increased, so that the separation selectivity and the mass transfer rate of a hydration reaction are improved, under the action of a liquid inlet distributor at the upper part of a separation tower, the separation liquid flows down along a flat membrane shape of a spiral channel, mixed gas with the pressure of 6 ~ 14 MPa is introduced from the bottom of the tower and is in countercurrent contact with the separation liquid along the spiral channel, and hydrates are quickly generated and flow to.
A method for quickly and continuously hydrating and separating coal bed gas comprises the following steps:
(1) Vacuumizing: vacuumizing the gas buffer tank, the hydration separation tower and the decomposer by using a vacuum pump to ensure that the gas buffer tank, the hydration separation tower and the decomposer meet the required vacuum degree requirement;
(2) Feeding, namely opening a gas cylinder, feeding a raw material gas into a gas buffer tank to 1 ~ 5MPa by a pressure reducing valve and a stop valve, then opening a refrigeration system, pre-cooling the raw material gas to 273 ~ 276K by a cooling jacket outside the gas buffer tank, opening a feeding port on a separation liquid storage tank, and filling the separation liquid into the separation liquid storage tank;
(3) Opening a first liquid level monitoring device, a second liquid level monitoring device and a third liquid level monitoring device, setting liquid level parameters, controlling an electromagnetic valve and a liquid delivery pump to be opened by the first liquid level monitoring device, opening a stop valve to feed liquid from a liquid inlet to a hydration separation tower, adjusting the flow rate of the feed liquid, observing through a window, enabling the feed liquid to flow down along a spiral channel in the separation tower in a liquid film mode, starting the electromagnetic valve and a solid-liquid mixed delivery pump when the liquid level at the bottom of the separation tower reaches a set value of the second liquid level monitoring device, delivering the feed liquid to a decomposer, opening the electromagnetic valve when the liquid level in the equally-dividing device reaches a set value of the third liquid level monitoring device, enabling the separation liquid to flow back to a separation liquid storage tank downwards, then opening a refrigeration system of the separation liquid storage tank, opening a heating system on the decomposer, and pre-cooling the separation liquid to;
(4) And (2) separating, namely opening a refrigeration system of the hydration separation tower, setting a backpressure value of a backpressure valve, then opening a stop valve, enabling a pressurization system and the stop valve to intake air to the hydration separation tower from an air inlet to enable the air to be in countercurrent contact with separation liquid along a spiral channel, keeping the temperature in the tower at 273 ~ 276K and the absolute pressure at 6 ~ 14 MPa, enabling the easily-hydrated component methane in the mixed gas to quickly react with the separation liquid to generate hydrate, enabling the hydrate to flow to the tower bottom in a slurry form, enabling the unhydrated component nitrogen to rise to the tower top, opening the backpressure valve to enable the nitrogen-rich gas to be dried from a nitrogen-rich gas outlet through a second gas dryer and be recorded by a third gas flowmeter and then be discharged, enabling the hydrate slurry to be conveyed to a decomposer from a tower bottom hydrate slurry outlet through a solid-liquid mixed conveying pump to decompose the methane-rich gas, enabling the methane-rich gas to pass through a one-way check valve, enabling the first gas dryer to be dried and be recorded by the second gas flowmeter and then to be discharged out of.
In the method, the separation liquid is a water-in-oil emulsion, methane in the mixed gas is selectively dissolved, the contact area of the methane gas and water is increased, the water phase in the emulsion is dispersed in an oil phase in the form of droplets of 2 ~ 10 mu m, the water content of the emulsion is 30vol% ~ 80 vol%, the oil phase is one or a mixture of long paraffin hydrocarbons such as hexane, heptane, octane, nonane, decane, diesel oil, gasoline, crude oil, white oil and the like, the emulsifier is a single emulsifier or a composite emulsifier with an HLB value of 3 ~ 10, and the emulsifier comprises a Span type or a composite emulsifier of the Span type and Tween type and other lipophilic surfactants or a composite system of the lipophilic surfactants and hydrophilic surfactants.
In the method, the hydrate slurry is a solid-liquid mixture of oil phase wrapped with fine hydrate particles, the particle size of the hydrate is 3 ~ 20 microns, under the action of an emulsifier on the interface of the oil phase and the hydrate particles, the situation that the hydrate particles are aggregated and further agglomerated to block a pipeline and the like, which are not beneficial to continuous operation, is avoided, and the fluidity of the hydrate slurry is greatly improved.
Compared with the prior art, the invention has the following advantages:
The method uses the water-in-oil emulsion to hydrate and separate the coal bed gas, so that the methane gas and the nitrogen gas are separated. Because nitrogen is difficult to dissolve in the oil phase, methane is easy to dissolve in the oil phase, so that the methane is dissolved in the oil phase, and the contact area of the methane and water is increased. And the coal bed gas is in countercurrent contact with the separation liquid flowing down in a film shape in the ascending process in the spiral channel in the separation tower, and the hydration reaction heat is removed more quickly while the mass transfer is accelerated due to the large contact area and the flowing material. The method can greatly improve the separation selectivity and the mass transfer rate of the hydration reaction, accelerate the generation of the hydrate and improve the separation efficiency.
Compared with the separation technologies such as a cryogenic method, an adsorption method, a membrane separation method and the like applied in the industry at present, the method has the advantages of good separation effect, low energy consumption, reusable separation liquid, environmental friendliness, simple process and the like.
compared with the existing intermittent hydration separation method, the method realizes continuous separation operation, can greatly improve the airspeed of the hydration separation reactor, improves the production efficiency, and has wide industrial application prospect.
Drawings
FIG. 1 is a schematic view of a device for quickly and continuously hydrating and separating coal bed gas provided by the invention.
FIG. 2 is a schematic diagram of a feed inlet distributor of a hydration separation tower.
FIG. 3 is a schematic diagram of the spiral channel structure in the hydration separation column.
The various components in the figure are as follows: the system comprises a gas cylinder 1, a pressure reducing valve 2, a gas buffer tank 4, a pressure gauge 6, a pressurization system 9, a first gas flowmeter 10, a gas inlet 12, a hydrate slurry outlet 14, a second liquid level monitoring device 15, a solid-liquid mixed transfer pump 17, a decomposer 18, a one-way check valve 21, a first gas dryer 22, a second gas flowmeter 23, a methane-rich gas outlet 24, a third liquid level monitoring device 25, a charging port 28, a separation liquid storage tank 30, a first liquid level monitoring device 31, a liquid delivery pump 32, a liquid flowmeter 35, a liquid inlet 37, a hydration separation tower 38, a temperature and pressure monitoring system 39, a window 40, a nitrogen-rich gas outlet 41, a back pressure valve 43, a second gas dryer 44, a third gas flowmeter 45, a nitrogen-rich gas outlet 46, a cooling liquid inlet 47, a cooling liquid outlet 48, a spiral passage 49, an equipartition device upstream baffle 50, an equipartition device downstream baffle 51, an in-tower, A separation column cooling jacket 53, a first stop valve 3, a second stop valve 8, a third stop valve 11, a fourth stop valve 36, a first electromagnetic valve 16, a second electromagnetic valve 26, a third electromagnetic valve 33, a first vent valve 7, a second vent valve 20, a third vent valve 42, a first drain port 13, a second drain port 27, a third drain port 34, a first thermometer 5, a second thermometer 19, and a third thermometer 29.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
The system comprises a gas cylinder 1, a gas pressure reducing valve 2, a gas buffer tank 4, a pressurization system 9, a first gas flow meter 10, a second gas flow meter 10, a hydration and moisture separation system 18, a hydration and moisture separation system 32, a hydration and a moisture content control system 32, a hydration and a moisture content control system 32, a hydration and a moisture content control system 10, a moisture content control system 32, a moisture content meter 10, a first gas flow meter 10 is connected with a hydration and moisture content monitor system 38, a moisture content monitor 30, a moisture content monitor 30, a moisture content monitor 30, a moisture content monitor, a moisture content monitor, a moisture content monitor, a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture content monitor a moisture.
A method for quickly and continuously hydrating and separating coal bed gas utilizes the characteristic that nitrogen is difficult to dissolve in an oil phase and methane is easy to dissolve in the oil phase, adopts water-in-oil emulsion as a separation liquid to dissolve methane in the oil phase, then the methane is contacted and dissolved with small water beads distributed in the oil phase, the contact area of the methane and water is increased, so that the separation selectivity and the mass transfer rate of a hydration reaction are improved, under the action of a uniform distributor at a liquid inlet 37 at the upper part of a separation tower, the separation liquid flows down along a spiral channel 49 in a flat film mode, mixed gas of 6 ~ 14 MPa is introduced from the bottom of the tower and is in countercurrent contact with the separation liquid along the spiral channel 49, and hydrate is quickly generated and flows to.
The using process of the invention is as follows:
(1) vacuumizing: the gas buffer tank 4, the hydration separation tower 38 and the decomposer 18 are vacuumized by a vacuum pump to meet the required vacuum degree.
(2) and feeding, namely opening the gas cylinder 1, feeding the raw material gas into the gas buffer tank 4 to 1 ~ 5MPa by using the pressure reducing valve 2 and the stop valve 3, then opening the refrigeration system, precooling the raw material gas to the required temperature of 273 ~ 276K by using a cooling jacket outside the gas buffer tank 4, opening the feeding port 28 on the separation liquid storage tank 30, and filling the separation liquid into the separation liquid storage tank 30.
(3) and (3) realizing separation liquid circulation, namely opening the first liquid level monitoring device 31, the second liquid level monitoring device 15 and the third liquid level monitoring device 25, setting liquid level parameters, then controlling the electromagnetic valve 33 and the liquid delivery pump 32 to be opened by the first liquid level monitoring device 31, opening the stop valve 36 to feed liquid from the liquid inlet 37 to the hydration separation tower 38, adjusting the flow rate of the feed liquid, observing through a window 40, and enabling the feed liquid to flow down along a spiral channel 49 in the separation tower 38 in a liquid film mode, when the liquid level at the bottom of the tower reaches the set value of the second liquid level monitoring device 15, opening the electromagnetic valve 16 and the solid-liquid mixed delivery pump 17 to deliver the feed liquid to the decomposer 18, when the liquid level in the equally decomposing device 18 reaches the set value of the third liquid level monitoring device 25, opening the electromagnetic valve 26, enabling the separation liquid to flow back to the separation liquid storage tank 30, then opening a refrigerating system of the separation liquid storage tank 30, opening a heating system on the decompos.
(4) and (3) separating, namely opening a refrigerating system of the hydration separation tower 38, setting a back pressure value of a back pressure valve 43, then opening a stop valve 8, introducing air from an air inlet 12 to the hydration separation tower 38 by a pressure-increasing system 9 and the stop valve 11, enabling the air to be in countercurrent contact with a separation liquid along a spiral passage 49, keeping the temperature in the tower at 273 ~ 276K and the absolute pressure at 6 ~ 14 MPa, enabling an easily-hydrated component (methane) in the mixed gas to be in contact with the separation liquid (water-in-oil emulsion) to quickly generate hydrate, enabling the hydrate to flow to the tower bottom in a slurry mode, enabling an unhydrated component (nitrogen) to rise to the tower top, opening the back pressure valve 43 to enable the nitrogen-rich gas to be discharged from a nitrogen-rich gas outlet 41 after being dried by a second gas drier 44 and recorded by a third gas flow meter 45, enabling the hydrate slurry to be conveyed from a hydrate slurry outlet 14 at the tower bottom by a solid-liquid mixing pump 17 to a decomposer 18 to be decomposed to discharge the methane-rich gas, enabling the first gas drier 22 to be dried by a one-way check valve 21 and discharged after being recorded by a second gas flow meter 23.
Claims (10)
1. A device for quickly and continuously hydrating and separating coal bed gas is characterized by comprising a feeding gas circuit, a separation liquid circulation circuit, a hydrating separation tower (38), a nitrogen-rich gas circuit and a methane-rich gas circuit;
The hydration separation tower (38) is provided with an air inlet (12), a liquid inlet (37), a nitrogen-rich gas outlet (41), a hydrate slurry outlet (14), a cooling liquid inlet (47) and a cooling liquid outlet (48)
The feeding gas circuit comprises a gas bottle (1), a gas reducing valve (2), a gas buffer tank (4), a pressurization system (9), a first gas flowmeter (10), a first stop valve (3), a first emptying valve (7), a second stop valve (8) and a third stop valve (11); the gas cylinder (1), the gas reducing valve (2), the gas buffer tank (4), the pressurization system (9) and the first gas flowmeter (10) are sequentially connected through a pipeline, and the first gas flowmeter (10) is connected with a gas inlet (12) of the hydration separation tower (38) through a pipeline; a first stop valve (3) is arranged between the gas pressure reducing valve (2) and the gas buffer tank (4), the top of the gas buffer tank (4) is connected with a first emptying valve (7) through a tee joint, a second stop valve (8) is arranged between the gas buffer tank (4) and the pressurization system (9), and a third stop valve (11) is arranged between the first gas flowmeter (10) and the hydration separation tower (38); the feeding gas circuit is connected to a gas inlet (12) of the hydration separation tower (38) through a pipeline;
The separation liquid circulating loop comprises a separation liquid storage tank (30), a first liquid level monitoring device (31), a liquid conveying pump (32), a liquid flow meter (35), a second liquid level monitoring device (15), a solid-liquid mixed conveying pump (17), a decomposer (18), a third liquid level monitoring device (25), a first electromagnetic valve (16), a second electromagnetic valve (26), a third electromagnetic valve (33), a second emptying valve (20), a second liquid discharging port (27), a feeding port (28), a third liquid discharging port (34) and a fourth stop valve (36); a liquid inlet (37) of the hydration separation tower (38) is sequentially connected with a liquid flowmeter (35) and a liquid delivery pump (32), and the liquid delivery pump (32) is connected with the bottom end of a separation liquid storage tank (30); a hydrate slurry outlet (14) of the hydration separation tower (38) is connected with the solid-liquid mixed transportation pump (17), the decomposer (18) and the separation liquid storage tank (30) in sequence; the first electromagnetic valve (16) is positioned on a pipeline between the hydration separation tower (38) and the solid-liquid mixed conveying pump (17) and is used for controlling the liquid level of the bottom in the hydration separation tower (38) in cooperation with the second liquid level monitoring device (15) and the solid-liquid mixed conveying pump (17); the second electromagnetic valve (26) is positioned on a pipeline between the decomposer (18) and the separation liquid storage tank (30) and is used for controlling the bottom liquid level in the decomposer (18) in cooperation with a third liquid level monitoring device (25); the third electromagnetic valve (33) is positioned on a pipeline between the separation liquid storage tank (30) and the liquid delivery pump (32) and is used for controlling the liquid level in the separation liquid storage tank (30) in cooperation with the first liquid level monitoring device (31) and the liquid delivery pump (32); the second emptying valve (20) is positioned on a right end pipeline of the top tee joint of the decomposer (18) and is used for emptying residual gas in the decomposer (18) at the end of operation; the second liquid outlet (27) is positioned on a right end pipeline of the tee joint at the bottom of the decomposer (18) and is used for discharging residual liquid in the decomposer (18) when the operation is finished; the feeding port (28) is positioned at the top of the separation liquid storage tank (30) and is used for feeding the separation liquid into the separation liquid storage tank (30); the third liquid outlet (34) is positioned on a right end pipeline of the tee joint at the bottom of the separation liquid storage tank (30) and is used for discharging residual liquid in the separation liquid storage tank (30) when the operation is finished; the fourth stop valve (36) is positioned on a pipeline between the liquid flow meter (35) and the liquid inlet (37); the first liquid level monitoring device (31) is positioned on the liquid level in the separation liquid storage tank (30), and controls the switch of the third electromagnetic valve (33) and the liquid delivery pump (32) through current signals; the second liquid level monitoring device (15) is positioned on the liquid level at the bottom in the hydration separation tower (38), and controls the switch of the first electromagnetic valve (16) and the solid-liquid mixed transportation pump (17) through current signals; the third liquid level monitoring device (25) is positioned on the liquid level in the decomposer (18) and controls the switch of the second electromagnetic valve (26) through a current signal;
A back pressure valve (43), a second gas dryer (44) and a third gas flowmeter (45) are connected to the nitrogen-rich passage, and a nitrogen-rich outlet (41) of the hydration separation tower (38) is connected with the back pressure valve (43), the second gas dryer (44) and the third gas flowmeter (45) in sequence;
And an outlet at the top of the decomposer (18) is connected with a one-way check valve (21), a first gas drier (22) and a second gas flowmeter (23) in sequence.
2. The device for quickly and continuously hydrating and separating the coal bed gas according to claim 1, wherein the buffer tank (4) is provided with a cooling jacket, a thermometer (5) and a pressure gauge (6) are connected to the buffer tank (4), and a first emptying valve (7) is connected to the top of the buffer tank.
3. The device for quickly and continuously hydrating and separating the coal bed gas according to claim 1, wherein the temperature and pressure conditions in the hydrate separation tower (38) are monitored by a temperature and pressure monitoring system (39), and a vent valve (42), a liquid discharge port (13) and a window (40) are further arranged on the hydrate separation tower (38).
4. the device for quickly and continuously hydrating and separating the coal bed gas according to claim 1, wherein the hydrating and separating tower (38) is a cylindrical tower reactor with a height-diameter ratio of 4 ~ 8:1, the inside of the reactor is of a spiral channel structure, the channel (49) is seamlessly welded with the pillar (52) and the inner wall of the separating tower, and the channel is coated with the hydrophobic nano-coating.
5. The device for quickly and continuously hydrating and separating the coal bed gas according to claim 1, wherein a box-shaped uniform distributor is arranged on the spiral channel (49) at the position of the liquid inlet (37), a nozzle of the liquid inlet is wrapped in the box-shaped uniform distributor, joints at the edge of the uniform distributor are all welded in a seamless mode, an upstream baffle plate (50) of the uniform distributor is a solid stainless steel plate, a downstream baffle plate (51) of the uniform distributor is a stainless steel plate with a plurality of grid-type small channels arranged at the lower edge, the width of each grid hole is 1 mm ~ 5 mm, and the height of each grid hole is 1 ~ 3 mm.
6. A rapid continuous hydration separation coal bed methane apparatus according to claim 1, characterized in that said decomposer (18) is placed at a position higher than the separation liquid storage tank (30), said decomposer (18) is a hydrate decomposition reactor with heating jacket, and is connected with a thermometer (19); the separation liquid storage tank (30) is provided with a cooling jacket.
7. A method for quickly and continuously hydrating and separating coal bed gas is characterized in that a water-in-oil emulsion is used as a separation liquid by utilizing the characteristic that nitrogen is difficult to dissolve in an oil phase and methane is easy to dissolve in the oil phase, so that the methane is dissolved in the oil phase and then is dissolved in contact with small water beads distributed in the oil phase, the contact area of the methane and water is increased, the separation selectivity and the mass transfer rate of a hydration reaction are improved, under the action of a uniform distributor of a liquid inlet (37) at the upper part of a separation tower, the separation liquid flows down along a spiral channel (49) in a film shape, mixed gas of 6 ~ 14 MPa is introduced from the bottom of the tower and is in countercurrent contact with the separation liquid along the spiral channel (49), and hydrate is quickly generated and flows to.
8. The method for hydration and separation of coal bed methane according to claim 7, which comprises the following steps:
(1) Vacuumizing: vacuumizing the gas buffer tank (4), the hydration separation tower (38) and the decomposer (18) by using a vacuum pump to meet the requirement of required vacuum degree;
(2) feeding, namely opening a gas cylinder (1), feeding a raw material gas into a gas buffer tank (4) to 1 ~ 5MPa by a pressure reducing valve (2) and a stop valve (3), then opening a refrigeration system, pre-cooling the raw material gas to 273 ~ 276K by a cooling jacket outside the gas buffer tank (4), opening a feeding port (28) on a separation liquid storage tank (30), and filling the separation liquid into the separation liquid storage tank (30);
(3) Opening a first liquid level monitoring device (31), a second liquid level monitoring device (15) and a third liquid level monitoring device (25), setting liquid level parameters, then controlling an electromagnetic valve (33) and a liquid delivery pump (32) to be opened by the first liquid level monitoring device (31), opening a stop valve (36) to feed liquid from a liquid inlet (37) to a hydration separation tower (38), adjusting the flow rate of the liquid inlet, observing through a window (40), enabling the liquid inlet to flow down along a spiral channel (49) in the separation tower (38) in a liquid film mode, when the liquid level at the bottom of the tower reaches the set value of the second liquid level monitoring device (15), opening an electromagnetic valve (16) and a solid-liquid mixed delivery pump (17), delivering the liquid to a decomposer (18), when the liquid level in the decomposer (18) reaches the set value of the third liquid level monitoring device (25), opening the electromagnetic valve (26), enabling the separation liquid to flow back to a separation liquid storage tank (30) downwards, then opening a refrigeration system of the separation liquid storage tank (30), opening a heating system on the decomposer (18), and realizing that the separation liquid jacket (~ K-273) is separated by the separation liquid outside;
(4) And (2) opening a refrigeration system of the hydration separation tower (38), setting a back pressure value of a back pressure valve (43), then opening a stop valve (8), introducing gas from a gas inlet (12) to the hydration separation tower (38) by a pressure boosting system (9) and the stop valve (11), enabling the gas to be in countercurrent contact with a separation liquid along a spiral channel (49) and rise up, keeping the temperature in the tower at 273 ~ 276K and the absolute pressure at 6 ~ 14 MPa, enabling the easy-to-hydrate component methane in the mixed gas to be in contact with the separation liquid to quickly generate hydrate, enabling the hydrate to flow to the tower bottom in a slurry form, enabling the unhydrated component nitrogen to rise to the tower top, opening the back pressure valve (43), enabling the nitrogen-rich gas to be dried from a nitrogen-rich gas outlet (41) through a second gas dryer (44) and be discharged after being recorded by a third gas flow meter (45), enabling the hydrate slurry to be conveyed from the hydrate slurry outlet (14) through a solid-liquid mixing pump (17) to a decomposer (18) to release the one-way methane-rich gas, enabling the hydrate slurry to flow to pass through a check valve (21), enabling the hydrate slurry to flow to be separated and flow back to a circulating storage tank (23), and enabling the hydrate to be discharged after being separated and being used for being.
9. The method for rapidly and continuously hydrating and separating the coal bed gas according to claim 8, wherein the separation liquid is a water-in-oil emulsion, the water phase in the emulsion is dispersed in the oil phase in the form of droplets of 2 ~ 10 μm, the water content of the emulsion is 30vol% to ~ 80 vol%, the oil phase is one or a mixture of hexane, heptane, octane, nonane, decane, diesel oil, gasoline, crude oil and white oil, the emulsifier is a single emulsifier or a composite emulsifier with an HLB value of 3 ~ 10, and the emulsifier comprises a Span emulsifier or a composite emulsifier of the Span emulsifier and a Tween emulsifier and other lipophilic surfactants or a composite system of the lipophilic surfactants and hydrophilic surfactants.
10. The method for rapidly and continuously hydrating and separating the coal bed gas according to claim 8, wherein the hydrate slurry is a solid-liquid mixture of oil phase and fine hydrate particles, and the particle size of the hydrate particles is 3 ~ 20 μm.
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