Treatment system for producing high salt water in coal bed gas and shale gas well

Abstract

The invention relates to a treatment system for producing high-salinity water from coal bed gas and shale gas wells. The treatment system comprises a high-salinity water tank, a pump, a filter tank, a heat exchanger, a reduction furnace, an oxidation furnace, a plurality of high-temperature microbubble evaporation crystallizers arranged in sequence, a gas-liquid separator, a dryer and a fresh water tank. The main heat source of the system is self-produced low-cost coal bed gas, a reduction furnace and an oxidation furnace are arranged, and the enrichment of high-concentration carbon dioxide is realized by utilizing a chemical combustion technology of a gas fuel oxygen carrier, so that the system is ensured to realize zero emission of carbon dioxide. Besides, the system adopts a high-temperature microbubble enhanced evaporation crystallizer, so that efficient separation of salt and resource recycling are achieved, the solid waste treatment cost is reduced, and meanwhile, the phenomena of scaling and blockage of equipment are effectively avoided. The system not only has a simple structure and less electrical equipment, but also can adopt a skid-mounted design, and is convenient to construct and operate at a coal bed gas wellhead.

Description

Technical Field

[0001] This invention belongs to the field of high-salinity wastewater treatment technology, specifically relating to a treatment system for high-salinity water produced from coalbed methane and shale gas wells. Background Technology

[0002] Because coal seams are generally located below aquifers, coalbed methane extraction releases large amounts of highly saline water. Direct discharge of this saline water not only wastes water resources but also pollutes the environment. In my country's water-scarce mining areas, the salinity of mine water far exceeds the discharge standard of 1000 mg / L, and its high mineralization makes it unsuitable for production and domestic use using conventional treatment methods. Direct discharge would lead to soil salinization, plant withering and death, and ultimately damage the ecological environment.

[0003] The requirements for the treatment and resource utilization of high-salinity water produced from coalbed methane wells have been elevated to the national level. In November 2020, the Ministry of Ecology and Environment, the National Development and Reform Commission, and the National Energy Administration issued the "Notice on Further Strengthening the Management of Environmental Impact Assessment for Coal Resource Development" (Environmental Impact Assessment

[2020] No. 63), requiring that mine water should be given priority for project construction and production, encouraging the use of mine water through multiple channels, and setting discharge standards for excess high-salinity water that needs to be discharged, stipulating that its salt content should not exceed 1000 mg / L. In water-scarce mining areas with drought and little rainfall, the treatment and reuse of high-salinity water can not only improve the compliance rate of wastewater discharge in mining areas and reduce environmental pollution, but also alleviate the water pressure in mining areas, save water resources, and improve the comprehensive utilization efficiency of water resources.

[0004] With increasingly stringent environmental policies, "zero discharge" of high-concentration brine has become an essential path for the survival of enterprises and coal mines. Currently, there are no reported engineering demonstrations of "zero discharge" treatment for high-salinity coalbed methane wells, and similar demonstrations for high-mineralization mine water are also rare. While completed projects can achieve the "zero discharge" goal, the processes need optimization, certain key technologies still require improvement, project construction investment is high, and operating and treatment costs are high, placing enormous pressure on enterprises. An even more prominent problem is that crystalline salt is a mixed salt, which is classified as hazardous waste, produced in large quantities, occupies a large area, and has few readily available hazardous waste treatment centers. The treatment of mixed salts has become a new challenge for enterprises. Summary of the Invention

[0005] To address the aforementioned issues, this invention proposes a treatment system for high-salinity produced from coalbed methane and shale gas wells. The system's primary heat source is self-produced, low-cost coalbed methane. It employs chemical looping combustion technology with a gaseous fuel oxygen carrier to achieve high-concentration carbon dioxide enrichment, ensuring zero carbon dioxide emissions. Furthermore, the system utilizes a high-temperature microbubble-enhanced evaporation crystallizer, achieving efficient salt separation and resource reuse, reducing solid waste treatment costs, and effectively preventing equipment scaling and clogging. This system features a simple structure and minimal electrical equipment, allowing for skid-mounted design for easy construction and operation at coalbed methane wellheads.

[0006] To achieve the above objectives, the present invention adopts the following technical solution: a treatment system for high-salinity water produced from coalbed methane and shale gas wells includes a high-salinity water tank, a pump, a filter tank, heat exchanger A, heat exchanger B, a reduction furnace, an oxidation furnace, multiple sequentially arranged high-temperature microbubble evaporators and crystallizers, gas-liquid separator A, gas-liquid separator B, a dryer, and a freshwater tank; the high-salinity water produced from the coalbed methane well enters the high-salinity water tank, the outlet of the high-salinity water tank is connected to the inlet of the pump, and the outlet of the pump is connected to the inlet of the filter tank; the high-salinity water outlet of the filter tank is divided into two paths, one of which is connected to the tube of heat exchanger A. One path connects to the tube-side inlet of heat exchanger A, and the other path connects to the tube-side inlet of heat exchanger B; the tube-side outlets of heat exchangers A and B are respectively connected to the high-salt inlet of the first high-temperature microbubble evaporator crystallizer via automatic regulating valve 1 and automatic regulating valve 2; the high-temperature microbubble evaporator crystallizers are arranged in series, wherein the high-salt outlet of the previous high-temperature microbubble evaporator crystallizer is connected to the high-salt inlet of the next high-temperature microbubble evaporator crystallizer via an automatic regulating valve; the wet salt outlet of the high-temperature microbubble evaporator crystallizer is connected to the wet salt inlet of the dryer; the coal seam produced by the coalbed methane well The gas enters the reduction furnace to reduce the high-temperature oxygen carrier into elemental form. The resulting high-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-1). The elemental oxygen carrier enters the oxidation furnace from the reduction furnace outlet. In the oxidation furnace, the oxygen carrier reacts with air, and the resulting high-temperature flue gas is divided into three paths. The first path of high-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-4). The flue gas outlet (6-2) of the first high-temperature microbubble evaporator crystallizer is connected to the inlet of gas-liquid separator A. The outlet of the gas separator is connected to the shell-side inlet of heat exchanger A, and the freshwater outlet of gas-liquid separator A is connected to the inlet of the freshwater tank; the flue gas outlet (6-3) of the first high-temperature microbubble evaporator crystallizer is connected to the inlet of gas-liquid separator B, the gas outlet of gas-liquid separator B is connected to the shell-side inlet of heat exchanger B, and the freshwater outlet of gas-liquid separator B is connected to the inlet of the freshwater tank; the second high-temperature flue gas from the oxidizer enters the subsequent high-temperature microbubble evaporator crystallizer, and the flue gas outlet of the subsequent high-temperature microbubble evaporator crystallizer is connected to the inlet of gas-liquid separator B; the third high-temperature flue gas from the oxidizer enters the dryer.

[0007] Furthermore, the sludge filtered by the filtration tank enters the sludge pyrolysis furnace and is pyrolyzed by the high-temperature flue gas of the reduction furnace. The pyrolysis gas produced is used as fuel for the reduction furnace, and the dried sludge after pyrolysis can be directly landfilled or used for road paving.

[0008] Furthermore, the first high-temperature microbubble evaporator crystallizer is equipped with two evaporation chambers, each with an independent flue gas inlet and outlet, and the two flue gases are not interconnected.

[0009] Furthermore, the flue gas inlet pipe of the high-temperature microbubble evaporation crystallizer is equipped with an automatically adjustable telescopic device. The flue gas inlet pipe can automatically adjust its length according to the change of the high brine level, thereby maintaining a constant immersion depth in the high brine.

[0010] Furthermore, the flue gas inlet pipe of the high-temperature microbubble evaporator crystallizer is equipped with a distribution plate at the bottom to disperse the flue gas into tiny bubbles.

[0011] Furthermore, the high-temperature microbubble evaporator crystallizer is equipped with an online salinity monitor, which is linked to an automatic regulating valve connected to the high-salinity outlet of the high-temperature microbubble evaporator crystallizer. The salinity inside the high-temperature microbubble evaporator crystallizer is maintained within a set range by controlling the opening degree of the automatic regulating valve.

[0012] Furthermore, the salt crystallized at the bottom of the high-temperature microbubble evaporator is conveyed to the dryer for drying using a spiral conveyor.

[0013] Furthermore, the flue gas discharged from the shell side outlet of heat exchanger A is composed of carbon dioxide, which can be used to make dry ice for sale; the flue gas discharged from the shell side outlet of heat exchanger B is composed of nitrogen and oxygen and is directly discharged into the atmosphere.

[0014] Furthermore, the reduction furnace and the oxidation furnace are coupled fluidized beds with gaseous fuel oxygen carriers.

[0015] Compared with the prior art, the present invention has the following beneficial effects:

[0016] 1. This system features a simple structure and requires minimal electrical equipment. Its skid-mounted design facilitates construction and operation at coalbed methane wellheads. The system can directly utilize its own produced coalbed methane as fuel, effectively reducing energy costs.

[0017] 2. The system is equipped with a reduction furnace and an oxidation furnace, and adopts gaseous fuel oxygen carrier chemical loop combustion technology. The oxygen carrier effectively transfers oxygen from the air to the coalbed methane, avoiding direct contact between the coalbed methane and air. This ensures that the generated carbon dioxide is not diluted, making carbon dioxide capture more efficient and convenient, and achieving the goal of "zero CO2 emissions".

[0018] 3. The system adopts a coupled process of high-temperature microbubble enhanced evaporation and fractional crystallization, which realizes efficient separation of salt and resource reuse, and reduces the cost of solid waste treatment. In the high-temperature microbubble enhanced evaporation crystallizer, the flue gas enters the high saline water in the form of microbubbles, thereby avoiding the phenomenon of equipment scaling and blockage.

[0019] 4. The high-temperature microbubble enhanced evaporation crystallizer of this system is equipped with an automatic adjustment device for the flue gas inlet pipe with constant immersion depth, ensuring that the evaporation rate of the crystallizer remains constant and the heat of the flue gas can be effectively utilized. In addition, an online salinity monitor is installed on the crystallizer and used in conjunction with the flow regulating valve to maintain the salinity in the crystallizer within the crystallization solubility range of a specific salt, thereby achieving continuous production of the system.

[0020] 5. The high-salinity filter material of this system is pyrolyzed at high temperature, converting the organic matter in it into pyrolysis gas for reuse, thereby achieving the harmless discharge of sludge.

[0021] 6. The number of crystallizers in this system's high-temperature microbubble enhanced crystallizer can be flexibly adjusted according to the salinity composition of the high-salinity water produced during coalbed methane extraction. This allows the system to adapt to different types of high-salinity water with relatively minor equipment modifications. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of a high-salinity treatment system for coalbed methane and shale gas wells according to the present invention.

[0023] In the diagram, 1-high saline pool, 2-filtration pool, 3-sludge pyrolysis furnace, 4-reduction furnace, 5-oxidation furnace, 6-first high-temperature microbubble evaporator crystallizer 1, 6-1-flue gas inlet 1, 6-2-flue gas outlet 1, 6-3-flue gas inlet 2, 6-4-flue gas outlet 2, 7-second high-temperature microbubble evaporator crystallizer, 8-third high-temperature microbubble evaporator crystallizer, 9-fourth high-temperature microbubble evaporator crystallizer, 10-fifth high-temperature microbubble evaporator crystallizer, 11-gas-liquid separator A, 12-heat exchanger A, 13-gas-liquid separator B, 14-heat exchanger B, 15-freshwater pool, 16-dryer, 17-pump, 18-online salinity monitor. Detailed Implementation

[0024] To better understand the technical essence and beneficial effects of the present invention, the specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

[0025] Example 1

[0026] Combination Figure 1The present invention discloses a treatment system for high-salinity water produced from coalbed methane and shale gas wells, comprising a high-salinity water tank (1), a pump (17), a filter tank (2), heat exchangers A (12), B (14), a reduction furnace (4), an oxidation furnace (5), multiple sequentially arranged high-temperature microbubble evaporation crystallizers, gas-liquid separator A (11), gas-liquid separator B (13), a dryer (16), and a freshwater tank (15); the high-salinity water produced from the coalbed methane well enters the high-salinity water tank (1), the outlet of the high-salinity water tank (1) is connected to the inlet of the pump (17), and the outlet of the pump (17) is connected to the inlet of the filter tank (2); the filter tank (2) contains high-salinity water. The outlet is divided into two paths, one connected to the tube-side inlet of heat exchanger A (12) and the other connected to the tube-side inlet of heat exchanger B (14); the tube-side outlets of heat exchanger A (12) and heat exchanger B (14) are respectively connected to the high-salt water inlet of the first high-temperature microbubble evaporator (6) through automatic regulating valve 1 and automatic regulating valve 2; the high-temperature microbubble evaporators are arranged in series, wherein the high-salt water outlet of the previous high-temperature microbubble evaporator is connected to the high-salt water inlet of the next high-temperature microbubble evaporator through an automatic regulating valve; the wet salt outlet of the high-temperature microbubble evaporator is connected to the wet salt inlet of the dryer (16); The coalbed methane produced from the coalbed methane well enters the reduction furnace (4) to reduce the high-temperature oxygen carrier into elemental substances. The resulting high-temperature flue gas enters the high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-1). The oxygen carrier elemental substances enter the oxidation furnace through the outlet of the reduction furnace. In the oxidation furnace, the oxygen carrier elemental substances react with air, and the resulting high-temperature flue gas is divided into three paths. The first path of high-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-4). The flue gas outlet (6-2) of the first high-temperature microbubble evaporator crystallizer is connected to the inlet of the gas-liquid separator A (11), and the gas outlet of the gas-liquid separator A (11) is connected to the shell-side inlet of the heat exchanger A (12). The gas-liquid separator A (11) is connected to the freshwater pool inlet at its freshwater outlet; the flue gas outlet (6-3) of the first high-temperature microbubble evaporator crystallizer is connected to the inlet of the gas-liquid separator B (13); the gas outlet of the gas-liquid separator B (13) is connected to the shell-side inlet of the heat exchanger B (14); the freshwater outlet of the gas-liquid separator B (13) is connected to the inlet of the freshwater pool (15); the second high-temperature flue gas from the oxidizer (5) enters the subsequent high-temperature microbubble evaporator crystallizer; the flue gas outlet of the subsequent high-temperature microbubble evaporator crystallizer is connected to the inlet of the gas-liquid separator B (13); the third high-temperature flue gas from the oxidizer (5) enters the dryer (16).

[0027] In the embodiment, the sludge filtered by the filter pool (2) is pyrolyzed by the high-temperature flue gas of the original furnace (4) in the sludge pyrolysis furnace (3). The pyrolysis gas generated is used as fuel for the reduction furnace (4). The dried sludge after pyrolysis can be directly landfilled or used for road paving.

[0028] In this embodiment, the first high-temperature microbubble evaporator crystallizer (6) is provided with two evaporation chambers, each of which has an independent flue gas inlet and outlet, and the two flue gases are not interconnected.

[0029] In this embodiment, the flue gas inlet pipe of the high-temperature microbubble evaporation crystallizer is equipped with an automatically adjustable telescopic device. The flue gas inlet pipe can automatically adjust its length according to the change of the high saline liquid level, thereby maintaining a constant immersion depth in the high saline liquid.

[0030] In this embodiment, a distribution plate is provided at the bottom of the flue gas inlet pipe of the high-temperature microbubble evaporator crystallizer to disperse the flue gas into tiny bubbles.

[0031] In this embodiment, the high-temperature microbubble evaporator crystallizer is equipped with an online salinity monitor (18), which is linked to an automatic regulating valve connected to the high-salinity outlet of the high-temperature microbubble evaporator crystallizer. By controlling the opening of the automatic regulating valve, the salinity in the high-temperature microbubble evaporator crystallizer is kept within a set range, thereby realizing continuous production of the system.

[0032] In this embodiment, the salt crystallized at the bottom of the high-temperature microbubble evaporator crystallizer is conveyed to the dryer (16) for drying by a spiral conveyor.

[0033] In this embodiment, the flue gas discharged from the shell side outlet of heat exchanger A (12) is composed of carbon dioxide, which can be used to make dry ice for sale; the flue gas discharged from the shell side outlet of heat exchanger B (14) is composed of nitrogen and oxygen and is directly discharged into the atmosphere.

[0034] In this embodiment, the reduction furnace (4) and the oxidation furnace (5) are a fluidized bed coupled with a gaseous fuel oxygen carrier.

[0035] In the embodiments, the system's simple structure and fewer electrical devices enable it to be skid-mounted, facilitating its construction and operation at coalbed methane wellheads.

[0036] In the embodiments, the high-temperature microbubble enhanced crystallizer of the system can flexibly adjust the number of crystallizers according to the salt composition of the high-salt water generated during coalbed methane mining.

[0037] Example 2

[0038] This embodiment is based on a daily processing capacity of 200m³. 3 Taking high-salinity coalbed methane production as an example, the calorific value of the coalbed methane at the wellhead is 7985 kcal / Nm³. 3 The reduction furnace (4) and the oxidation furnace (5) are circulating fluidized beds, in which the oxygen carrier is Fe2O3.

[0039] High saline solution at 8.33m 3A flow rate of / h is pumped from the high-salinity tank (1) to the filter tank (2) by pump (17) for solid-liquid separation. The filter residue then enters the sludge pyrolysis furnace (3), where it is pyrolyzed to produce 0.03m³ of sludge. 3 / h of pyrolysis gas. This pyrolysis gas is mixed with 750m³ of... 3 / h of coalbed methane enters the reduction furnace (4) together to generate 2250m³. 3 High-temperature flue gas per hour. The metallic iron (Fe) generated during the reduction process is transported to the oxidation furnace (5), where it undergoes an oxidation reaction under the influence of air, generating 2800m³ / h of high-temperature flue gas. 3 / h of high-temperature flue gas and ferric oxide (Fe2O3). The generated Fe2O3 is then fed back to the reduction furnace (4) to participate in subsequent reduction reaction cycles.

[0040] The 2250m produced by the reduction furnace (4) 3 High-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer (6) through the flue gas inlet (6-1). Inside the crystallizer, the flue gas is dispersed into tiny bubbles, fully contacting the high-salt water and promoting efficient evaporation of water. The evaporated flue gas, carrying water vapor, is discharged through the flue gas outlet (6-2) and enters the gas-liquid separator A (11) for gas-liquid separation. The separated fresh water, 4.5 tons / h, is discharged into the fresh water pool (15) for reuse, while the flue gas (mainly composed of CO2) enters the heat exchanger A (12) and reacts with the filtered 3.7m³ / h water. 3 The high-temperature brine is used for heat exchange, generating 1480 kg / h of CO2 that can be sold externally. The high-temperature brine after heat exchange enters the first high-temperature microbubble evaporator crystallizer (6) through the automatic regulating valve 1.

[0041] The 2800m produced by the oxidation furnace (5) 3 The high-temperature flue gas is divided into three streams, the first stream being 1000m³ / h. 3 High-temperature flue gas per hour enters the first high-temperature microbubble evaporator crystallizer (6) through the flue gas inlet (6-4). Inside the crystallizer, the flue gas is dispersed into tiny bubbles, fully contacting the high-salt water and promoting efficient evaporation of water. The evaporated flue gas, carrying water vapor, is discharged through the flue gas outlet (6-3) and, together with the flue gas discharged from the second to fifth high-temperature microbubble evaporator crystallizers, enters the gas-liquid separator B (13) for gas-liquid separation. The separated fresh water, 3.5 tons / hour, is discharged into the fresh water pool (15) for reuse, while the flue gas enters the heat exchanger B (14) and is filtered to obtain 4.63 m³ of fresh water. 3 The high-temperature brine is used for heat exchange, and the brine after heat exchange enters the first high-temperature microbubble evaporator crystallizer (6) through the automatic regulating valve 2. The flue gas (composed of O2 and N2) can be directly discharged into the atmosphere. The second high-temperature flue gas serves as the heat source for the evaporation and crystallization processes of the second, third, fourth, and fifth high-temperature microbubble evaporators crystallizers. The third high-temperature flue gas is used in the dryer (16) for drying wet salt, providing the necessary heat energy to ensure the effective drying of wet salt.

[0042] Salt 1, crystallized in the first high-temperature microbubble evaporator (6), is transported by a screw conveyor to a dryer (16) for drying, yielding a salt 1 product with a yield of 126 kg / h. The concentrated high-salt water volume is 3.83 m³. 3 Salt 2, produced at a rate of 170 kg / h, flows from the first high-temperature microbubble evaporator crystallizer (6) through the automatic regulating valve 3 into the second high-temperature microbubble evaporator crystallizer (7). The salt 2 precipitated from this re-evaporation and crystallization is then transported by a screw conveyor to the dryer (16) for drying, yielding a salt 2 product with a yield of 3.2 m³. The concentrated high-salt water... 3 The salt 3 produced by the second high-temperature microbubble evaporator crystallizer (7) flows into the third high-temperature microbubble evaporator crystallizer (8) via the automatic regulating valve 4. The salt 3 precipitated by the re-evaporation crystallization is then transported to the dryer (16) by a screw conveyor for drying, resulting in a salt 3 product of 229 kg / h. The concentrated high-salt water is 2.12 m 3 The salt 4 produced by the re-evaporation and crystallization process flows from the third high-temperature microbubble evaporator crystallizer (8) through the automatic regulating valve 5 into the fourth high-temperature microbubble evaporator crystallizer (9). The salt 4 precipitated from the re-evaporation and crystallization is then transported to the dryer (16) via a screw conveyor for drying, yielding a salt 4 product of 97 kg / h. The concentrated high-salt water is 1.49 m³. 3 The salt 5 produced by the fourth high-temperature microbubble evaporator crystallizer (9) flows into the fifth high-temperature microbubble evaporator crystallizer (10) through the automatic regulating valve 6. The salt 5 precipitated by the evaporation crystallizer is then transported to the dryer (16) by the screw conveyor for drying, and a salt 5 product of 1368 kg / h is obtained.

[0043] Of course, the above description is not intended to limit the present invention, and the present invention is not limited to the examples given above. Any changes made by those skilled in the art within the scope of the present invention are also within the protection scope of the present invention.

Claims

1. A treatment system for high-salinity produced from coalbed methane and shale gas wells, characterized in that, The system includes a high-salt water tank, a pump, a filter tank, heat exchanger A, heat exchanger B, a reduction furnace, an oxidation furnace, multiple sequentially arranged high-temperature microbubble evaporation crystallizers, gas-liquid separator A, gas-liquid separator B, a dryer, and a freshwater tank. High-salt water produced from the coalbed methane well enters the high-salt water tank. The outlet of the high-salt water tank is connected to the inlet of the pump, and the outlet of the pump is connected to the inlet of the filter tank. The high-salt water outlet of the filter tank is divided into two paths: one connected to the tube-side inlet of heat exchanger A, and the other connected to the tube-side inlet of heat exchanger B. The tube-side outlets of heat exchangers A and B are respectively connected to the high-salt water inlet of the first high-temperature microbubble evaporation crystallizer via automatic regulating valves 1 and 2. The high-temperature microbubble evaporation crystallizers are arranged in series, with the high-salt water outlet of the previous high-temperature microbubble evaporation crystallizer connected to the high-salt water inlet of the next high-temperature microbubble evaporation crystallizer via an automatic regulating valve. The wet salt outlet of the high-temperature microbubble evaporation crystallizer is connected to the wet salt inlet of the dryer. The coalbed methane produced from the coalbed methane well enters the reduction furnace to reduce the high-temperature oxygen carrier into elemental gas, producing… The high-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-1); the oxygen carrier enters the oxidation furnace from the outlet of the reduction furnace, where the oxygen carrier reacts with air, and the resulting high-temperature flue gas is divided into three paths. The first path of high-temperature flue gas enters the first high-temperature microbubble evaporator crystallizer through the flue gas inlet (6-4); the flue gas outlet (6-2) of the first high-temperature microbubble evaporator crystallizer is connected to the inlet of gas-liquid separator A, and the gas outlet of gas-liquid separator A is connected to the shell side of heat exchanger A. The gas-liquid separator A's freshwater outlet is connected to the freshwater pool inlet; the first high-temperature microbubble evaporator crystallizer's flue gas outlet (6-3) is connected to the gas-liquid separator B's inlet, the gas outlet of gas-liquid separator B is connected to the shell-side inlet of heat exchanger B, and the freshwater outlet of gas-liquid separator B is connected to the freshwater pool inlet; the second high-temperature flue gas from the oxidizer enters the subsequent high-temperature microbubble evaporator crystallizer, and the flue gas outlet of the subsequent high-temperature microbubble evaporator crystallizer is connected to the gas-liquid separator B's inlet; the third high-temperature flue gas from the oxidizer enters the dryer.

2. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The sludge filtered by the filtration tank enters the sludge pyrolysis furnace and is pyrolyzed by the high-temperature flue gas of the reduction furnace. The pyrolysis gas produced is used as fuel for the reduction furnace. The dried sludge after pyrolysis can be directly landfilled or used for road paving.

3. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The first high-temperature microbubble evaporator crystallizer has two evaporation chambers, each with an independent flue gas inlet and outlet, and the two flue gases are not interconnected.

4. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The flue gas inlet pipe of the high-temperature microbubble evaporation crystallizer is equipped with an automatically adjustable telescopic device. The length of the flue gas inlet pipe can be automatically adjusted according to the change of the high brine level, so as to keep the immersion depth in the high brine constant.

5. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The flue gas inlet pipe of the high-temperature microbubble evaporator crystallizer is equipped with a distribution plate at the bottom, which is used to break the flue gas into tiny bubbles.

6. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The high-temperature microbubble evaporator crystallizer is equipped with an online salinity monitor, which is linked to an automatic regulating valve connected to the high-salinity outlet of the high-temperature microbubble evaporator crystallizer. The salinity inside the high-temperature microbubble evaporator crystallizer is maintained within a set range by controlling the opening degree of the automatic regulating valve.

7. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The salt crystallized at the bottom of the high-temperature microbubble evaporator is transported to the dryer for drying using a spiral conveyor.

8. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The flue gas discharged from the shell side outlet of heat exchanger A is composed of carbon dioxide, which can be used to make dry ice for sale; the flue gas discharged from the shell side outlet of heat exchanger B is composed of nitrogen and oxygen and is directly discharged into the atmosphere.

9. The high-salinity treatment system for coalbed methane and shale gas wells according to claim 1, characterized in that, The reduction furnace and oxidation furnace are coupled fluidized beds with gaseous fuel oxygen carriers.

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