CN201688650U - Full liquification separation equipment for coalbed gas containing air - Google Patents
Full liquification separation equipment for coalbed gas containing air Download PDFInfo
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- CN201688650U CN201688650U CN2010201717254U CN201020171725U CN201688650U CN 201688650 U CN201688650 U CN 201688650U CN 2010201717254 U CN2010201717254 U CN 2010201717254U CN 201020171725 U CN201020171725 U CN 201020171725U CN 201688650 U CN201688650 U CN 201688650U
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- 238000000926 separation method Methods 0.000 title claims abstract description 235
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 252
- 239000007789 gas Substances 0.000 claims abstract description 152
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 124
- 238000001816 cooling Methods 0.000 claims abstract description 86
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 41
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 41
- 239000001301 oxygen Substances 0.000 claims abstract description 39
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 38
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 34
- 238000009833 condensation Methods 0.000 claims abstract description 30
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- 238000007906 compression Methods 0.000 claims abstract description 23
- 230000006835 compression Effects 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims description 147
- 239000003245 coal Substances 0.000 claims description 98
- 239000003949 liquefied natural gas Substances 0.000 claims description 31
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 17
- 238000000746 purification Methods 0.000 claims description 15
- 239000003507 refrigerant Substances 0.000 description 32
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 238000000034 method Methods 0.000 description 18
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- 238000004519 manufacturing process Methods 0.000 description 3
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- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model relates to full liquification separation equipment for coalbed gas containing air. The full liquification separation equipment comprises a compression purifying system, a cooling system and a liquification separation system and is characterized in that the liquification separation system comprises a double-layered hydrocarbon-oxygen separation tower and a nitrogen separation tower; the double-layered hydrocarbon-oxygen separation tower comprises an upper tower and a lower tower; a condensation evaporimeter is arranged between the upper tower and the lower tower; an outlet used for outputting nitrogen is formed at the top of the nitrogen separation tower; an inlet and an outlet are formed at the bottom of the nitrogen separation tower; a pipeline for conveying coalbed gas containing air sequentially passes through the compression purifying system and the cooling system and is connected to an inlet of the lower tower which allows the coalbed gas containing air to enter; an outlet at the top of the lower tower is connected with a first inlet at the top of the upper tower through a JT valve; an outlet at the top of the upper tower is connected with the inlet at the bottom of the nitrogen separation tower; and the outlet at the bottom of the nitrogen separation tower is connected with a second inlet at the top of the upper tower. By adopting the full liquification separation equipment, hydrocarbon, oxygen and nitrogen can be separated completely.
Description
Technical Field
The utility model relates to a splitter of coal bed gas especially relates to a full liquefaction splitter of coal bed gas that contains air.
Background
Coal bed gas, commonly known as gas, is obtained by adsorbing methane by coal bodies in the process of coal formation. The geological structure conditions in China are complex, high gas mines and coal and gas outburst mines are numerous, and only in national key coal mines, 45 percent of the coal and gas outburst mines are occupied. The gas is colorless, tasteless, inflammable and explosive, can be analyzed, separated and dispersed in the coal seam development process, and is extremely easy to cause explosion accidents when the gas concentration in the air is between 5.5 and 16 percent and open fire occurs. The method is a serious problem which puzzles coal mine safety production for a long time, and more than 80 percent of extra-large and serious accidents of coal mines in China are caused by gas. In addition, the direct discharge of methane into the atmosphere not only causes the greenhouse effect, but also has a destructive effect on the ozone layer.
Coal is mainly used in the primary energy structure of China for a long time, great pressure is brought to the environment, and under the condition that the oil price and gas price of the international market are high, the change of the energy consumption structure by means of massive import is not practical. By developing the coal bed gas (the main component is methane), the coal mine production safety problem can be solved, the energy structure can be improved, the pollution is reduced, and good economic benefit is obtained. Along with the more and more outstanding energy problem, the development and utilization of coal bed gas are also increasing the temperature continuously. The united states is in the leading position in the world in terms of research, exploration, development and utilization of coal bed gas, and is a country which is the first to obtain commercial development of coal bed gas. The development and utilization of the coal bed gas in China are rapid, and the initial commercial scale development is realized. Coal bed gas in China is mostly distributed in small gas fields with low reserves and dispersed distribution, so that the method is suitable for development and utilization by adopting a low-temperature liquefaction mode. The conventional natural gas and coal bed gas liquefaction process only focuses on how to liquefy hydrocarbon components, and the coal bed gas usually contains CO2Nitrogen, oxygen and other components, especially oxygen-containing coal bed gas, are the root cause of coal mine accidents in China, so how to safely and efficiently separate and treat the components is the key and difficult point of the coal bed gas liquefaction process.
There have been a variety of patent applications that are used for liquefaction separation technology and equipment of oxygen-containing coal bed gas at present, for example, chinese utility model patent No. 200620115881.2 discloses a liquefaction equipment of air-containing coal bed gas, including compression clarification plant, refrigeration plant and liquefaction splitter, liquefaction splitter has the heat exchanger, the hot medium access connection of heat exchanger among compression clarification plant and the liquefaction splitter, refrigeration plant and liquefaction splitter's refrigeration medium access connection, liquefaction splitter is including the heat exchanger and the two-stage fractionating tower that connect gradually, and first fractionating tower has the condenser, and the second fractionating tower has the evaporimeter, and its characterized in that, first fractionating tower top, bottom and second fractionating tower top, bottom pass through the pipeline and link to each other, and first fractionating tower condenser still has the gas pipeline and introduces gas into refrigeration plant. The utility model provides an equipment realizes the separation of coal bed gas through adopting the cryogenic rectification method to obtain liquefied natural gas. The utility model discloses a only obtain the LNG product, and do not realize the separation of nitrogen and oxygen, therefore must empty the air from the second fractionating tower top, therefore probably cause the waste. 200620134297.1 discloses a liquefaction separation equipment of coal bed gas containing air, the separation equipment that it provided need separate through two-stage fractionation, and the equipment that involves is more, process flow is more complicated, except obtaining the LNG product, still obtains high-purity nitrogen, still has some nitrogen, oxygen gas mixture to empty, obtains partly moreover and is gaseous product, still is not convenient for store the transportation.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, an object of the utility model is to provide a full liquefaction splitter of coal bed gas contains air, through the improvement to the knockout tower, has realized the complete liquefaction separation of liquefied natural gas, liquid oxygen and liquid nitrogen, has characteristics such as simple structure, separation effect are good, product purity height.
In order to achieve the above object, the utility model provides a full liquefaction splitter of coal bed gas that contains air, it includes compression clean system, cooling system and liquefaction piece-rate system, its characterized in that:
the liquefaction separation system comprises a double-layer hydrocarbon oxygen separation tower and a nitrogen separation tower, wherein the double-layer hydrocarbon oxygen separation tower consists of an upper tower and a lower tower, the lower tower is provided with an inlet for air-containing coal bed gas to enter, the bottom of the lower tower is provided with an outlet for outputting liquefied natural gas, the top of the lower tower is provided with an outlet, the top of the upper tower is provided with a second inlet and an outlet, the bottom of the upper tower is provided with an outlet for outputting liquid oxygen, and a condensation evaporator is arranged between the upper tower and the lower tower; the top of the nitrogen separation tower is provided with an outlet for outputting nitrogen, and the bottom of the nitrogen separation tower is provided with an inlet and an outlet; wherein,
a pipeline for conveying the coal bed gas containing air sequentially passes through the compression purification system and the cooling system and is connected to an inlet of the lower tower for the coal bed gas containing air to enter;
the top of the upper tower is provided with a first inlet, the outlet at the top of the lower tower is connected with the first inlet at the top of the upper tower through a JT valve, or the middle part of the nitrogen separation tower is provided with an inlet, and the outlet at the top of the lower tower is connected with the inlet at the middle part of the nitrogen separation tower through a JT valve; when the former scheme is adopted, an inlet does not need to be arranged in the middle of the nitrogen separation tower, and when the latter scheme is adopted, the first inlet is not arranged at the top of the upper tower;
an outlet at the top of the upper tower is connected with an inlet at the bottom of the nitrogen separation tower;
and an outlet at the bottom of the nitrogen separation tower is connected with a second inlet at the top of the upper tower.
In the above-mentioned total liquefaction separation apparatus, the outlet at the top of the nitrogen separation column may be connected to a conventional cryogenic cooling device or the cooling system for cooling the nitrogen gas to obtain liquid nitrogen.
In the full liquefaction separation equipment of the air-containing coal bed gas provided by the utility model, preferably, the liquefaction separation system is provided with a first gas-liquid separation tank, the bottom of the lower tower is provided with an inlet, wherein,
an outlet at the bottom of the lower tower is connected with an inlet of the first gas-liquid separation tank through a pipeline, and the pipeline passes through the cooling system;
an outlet (gas outlet) of the first gas-liquid separation tank is connected to an inlet at the bottom of the lower column, and the first gas-liquid separation tank further has an outlet (liquid outlet) for outputting liquefied natural gas.
In the full liquefaction separation equipment for air-containing coal bed gas provided by the present invention, preferably, the liquefaction separation system has a second gas-liquid separation tank, wherein the outlet at the top of the nitrogen separation tower passes through the cooling system through a pipeline and then is connected to the inlet of the second gas-liquid separation tank (i.e., the liquefaction separation system has a second gas-liquid separation tank, wherein the outlet at the top of the nitrogen separation tower is connected to the inlet of the second gas-liquid separation tank through a pipeline, and the pipeline passes through the cooling system first);
an outlet (gas outlet) of the second knockout drum is connected to the top inlet of the nitrogen separation column, and the second knockout drum further has an outlet (liquid outlet) that outputs liquid nitrogen.
In the above full liquefaction separation equipment, the compression purification system is used for performing compression purification on the air-containing coal bed gas, including filtration, acid gas removal, dehydration, mercury removal and the like, and a conventional system or device can be adopted.
The utility model provides an among the full liquefaction splitter of air-containing coal bed gas, double-deck hydrocarbon oxygen knockout tower mainly used separates hydrocarbons from air-containing coal bed gas. When the cooling system is used for recovering cold in the liquid hydrocarbon at the bottom of the lower tower, the method can be carried out in the following way: after the compressed, purified and cooled air-containing coal bed gas enters the lower tower from an inlet (the inlet is preferably arranged in the middle of the lower tower) for the air-containing coal bed gas to enter, liquid flows downwards (in the flowing process, the liquid exchanges heat and mass with the gas flowing upwards, nitrogen and oxygen in the liquid are gasified and enter the gas, hydrocarbon in the gas is condensed and enters the liquid, so that the hydrocarbon content in the liquid is higher and higher, the nitrogen and oxygen content in the gas is higher and higher, liquid hydrocarbon with high purity, namely liquefied natural gas, is obtained at a position close to the bottom of the lower tower and flows out from an outlet at the bottom of the lower tower, the liquid hydrocarbon can be conveyed into a cooling system through a pipeline, cold energy is output to refrigerant in the cooling system, the liquid is heated to evaporate part of the liquid to form hydrocarbon in a gas-liquid mixed state, and the liquid hydrocarbon is conveyed into a first gas-liquid separation tank for separation, wherein, the liquid hydrocarbon is exported to become a high-purity liquefied natural gas product (LNG product), and the gaseous hydrocarbon enters the lower tower through the inlet at the bottom of the lower tower and continues to participate in the liquefaction separation process (the part of the gaseous hydrocarbon can perform heat and mass exchange with the liquid flowing from top to bottom in the upward flowing process). In the lower column, the gas flows upwards and is condensed at the top of the lower column, the cold required is supplied by the reboiling of the liquid at the bottom of the upper column, and in fact, while the hydrocarbons are condensed, the liquid at the bottom of the upper column is heated as a result, and the condensing evaporator achieves the heat exchange between the liquid at the bottom of the upper column and the gas at the top of the lower column. In solitary knockout tower, generally, the bottom all is equipped with the reboiler, and the top all is equipped with the recondensor, the utility model provides a complete liquefaction splitter has adopted bilayer structure's oxygen gas knockout tower, combines two knockout towers of originally separating through the condensation evaporimeter together, has replaced a reboiler and a recondensor, has realized the combination of two towers, has reduced equipment quantity to the heat transfer difference in temperature of condensation evaporimeter can be controlled very little, thereby the cold volume and the heat that utilize high-efficiently. The upper column and the lower column are combined together by a condensing evaporator to constitute a double-layer hydrocarbon oxygen separation column, wherein the structure of the condensing evaporator is substantially the same as that of a conventional condensing evaporator, and the condensing evaporator can be applied as long as heat exchange between liquid at the bottom of the upper column and gas at the top of the lower column can be achieved. In the above-mentioned total liquefaction separation apparatus, the condensing evaporator may be connected to the upper and lower columns as a whole, that is, a single condensing evaporator unit (i.e., heat exchanger) may be arranged in the upper column or a plurality of condensing evaporator units may be arranged in a single-layer star shape in the upper column, or an auxiliary condensing evaporator may be provided outside the upper column; the condensation evaporator which is independently arranged can also be adopted, namely a plurality of condensation evaporator units are connected in parallel in a cylindrical container and are respectively connected with the upper tower and the lower tower by pipelines, wherein the heat exchange unit can adopt the structural forms of plate-fin type, tube array type, coil type and the like.
The utility model provides an among the full liquefaction splitter of air-containing coal bed gas, the gas that goes up the top of the tower gets into the bottom of the nitrogen separation tower through the entry of nitrogen separation tower bottom, and the liquid of nitrogen separation tower bottom gets into the tower by the second entry at double-deck hydrocarbon oxygen knockout tower top of the tower after the pump.
The utility model provides an among the full liquefaction splitter of coal bed gas that contains air, preferably, the export of nitrogen knockout tower top is through the pipeline and is passed through cooling system's second cold box and second gas-liquid separation jar's entry linkage. The gas (composed of high-purity nitrogen) flowing out of the outlet at the top of the nitrogen separation tower is cooled into liquid by the refrigerant in the cooling system, then passes through the second gas-liquid separation tank (used for protecting the pump under abnormal working conditions) and the pump, one part of the gas is output as a liquid nitrogen product, and the other part of the gas is taken as reflux liquid and enters the nitrogen separation tower through the inlet at the top of the nitrogen separation tower.
After entering an inlet at the upper part of the double-layer hydrocarbon oxygen separation tower, the liquid leaving from an outlet at the bottom of the nitrogen separation tower flows from top to bottom, and in the process, the liquid and the gas flowing from bottom to top are subjected to heat-mass exchange; from the top to the bottom of the upper tower, the nitrogen content gradually decreases and the oxygen content gradually increases, the bottom of the upper tower is heated and boiled by the evaporation side of the condensation evaporator, one part of liquid is vaporized and flows upwards, and the other part of unvaporized liquid is the liquid oxygen product with higher purity.
The utility model provides an among the full liquefaction splitter of coal bed gas that contains air, the compression clean system and the cooling system who adopt can adopt the system or the device commonly used in the art, preferably, cooling system adopts single-stage mixed refrigerant circulating device, make and contain air coal bed gas and get into liquefaction piece-rate system after first cooler and the second cooler that loops through single-stage mixed refrigerant circulating device cool off, this cooling system (single-stage mixed refrigerant circulating device promptly) includes one section compressor, one section air cooler, one section gas-liquid separation jar, two-stage compressor, two-stage air cooler, two-stage gas-liquid separation jar, first cooler and second cooler, one section gas-liquid separation jar has an entry, a top export (gas outlet) and a bottom export (liquid outlet), wherein:
the first section of compressor, the first section of air cooler, the inlet of the first section of gas-liquid separation tank, the bottom outlet of the first section of gas-liquid separation tank, the first cooling box (second flow passage), the first JT valve and the first cooling box (third flow passage) are sequentially connected to form a high-temperature cycle;
the first-stage compressor, the first-stage air cooler, the inlet of the first-stage gas-liquid separation tank, the top outlet of the first-stage gas-liquid separation tank, the second-stage compressor, the second-stage air cooler, the second-stage gas-liquid separation tank, the first cooling box (first flow channel), the second cooling box (second flow channel), the second JT valve, the second cooling box (third flow channel) and the first cooling box (third flow channel) are sequentially connected to form low-temperature circulation.
In the high-temperature cycle and the low-temperature cycle of the cooling system, the liquid refrigerant obtained after separation of the gas-liquid separation tank directly enters the first cooling tank to be pre-cooled (the temperature is about-70 ℃ to-90 ℃), the partial refrigerant passes through the first cooling tank and then is throttled by the first JT valve, then returns to the first cooling tank to provide cold for cooling the air-containing coal bed gas subjected to compression purification treatment, and pre-cools the liquid refrigerant and the gas refrigerant entering the first cooling tank (in full-liquefaction separation equipment, the operation of each part is continuously circulated); after passing through the second-stage compressor, the air cooler and the second-stage gas-liquid separation tank, the gas refrigerant obtained after separation of the first-stage gas-liquid separation tank enters the second cooling tank through the first cooling tank and is sequentially pre-cooled to a very low temperature (about-160 to-190 ℃), the part of the refrigerant is throttled by the second JT valve after passing through the second cooling tank and then returns to the second cooling tank to provide cold at a low temperature level, and the part of the refrigerant is mixed with the refrigerant throttled by the first JT valve after passing through the second cooling tank and enters the first cooling tank to provide cold at a high temperature level together, after the steps are completed, the refrigerant returns to the first-stage compressor and continues to circulate next step.
The utility model provides an among the full liquefaction splitter of coal bed gas that contains air, preferably, the pipeline of carrying the coal bed gas that contains air loops through compression clean system first cold box and the second cold box is connected to the entry that the tower confession contains the air coal bed gas entering down.
The utility model provides an among the full liquefaction splitter of air-bearing coal bed gas, preferably, the export at nitrogen separation tower top is through the pipeline and is passed through cooling system's second cold box (first flow path) with the entry linkage of second gas-liquid separation jar. The outlet pipe at the top of the nitrogen separation column first passes through the second cold tank (first flow path) to exchange heat and cold between the nitrogen gas therein and the refrigerant in the second cold tank, and then is connected to the inlet of the second knockout drum.
The utility model provides an among the complete liquefaction splitter of air-containing coal bed gas, preferably, the export of lower tower bottom is passed through the pipeline and is passed through cooling system's second cold box (fifth runner) and the entry linkage of first gas-liquid knockout drum. The pipeline at the bottom outlet of the lower tower firstly passes through the second cold box (the fifth flow channel) so that the liquefied natural gas in the second cold box and the refrigerant in the second cold box carry out cold-heat exchange, the cold energy in the liquefied natural gas is recovered, the liquefied natural gas is heated, part of the liquefied natural gas is evaporated into a gaseous state, and the pipeline is connected to the inlet of the first gas-liquid separation tank after passing through the second cold box.
The utility model provides an among the full liquefaction splitter, can have following two kinds of modes to realize the reboiling of bottom of tower down:
liquid from an outlet at the bottom of the lower tower passes through the second cold box, cold energy is provided for the second cold box, the second cold box is heated to realize reboiling, then gas-liquid separation is realized in the first gas-liquid separation tank, the liquid is output as liquefied natural gas, and the gas returns to the lower tower to flow from bottom to top;
it is also possible to provide a reboiler at the bottom of the lower column, which is connected to the outlet and inlet at the bottom of the lower column, and reboil the liquid at the bottom of the lower column by using external heat, for example, the outlet at the bottom of the lower column is connected to the reboiler, and heat is supplied to the reboiler in a conventional heating manner to boil part of the liquid in the reboiler and return the liquid to the lower column for upward flow, and the other part of the liquid is output as the liquefied natural gas product.
The utility model provides an among the full liquefaction splitter, can have following two kinds of modes to realize the condensation of the nitrogen gas of top of the tower output: enabling nitrogen from an outlet at the top of the upper tower to pass through a second cold box, and providing cold energy to the second cold box to condense the nitrogen to obtain liquid nitrogen; the conventional low-temperature cooling device and the condenser can be arranged to provide cold energy, so that the cold energy and the outlet at the top of the upper tower are condensed to obtain liquid nitrogen, and then the liquid nitrogen enters the gas-liquid separation tank for separation.
The utility model provides an among the full liquefaction splitter of air-containing coal bed gas, preferably, the export of nitrogen separation tower bottom with be equipped with a pump between the second entry of last top of the tower portion for the liquid of the export output of pump sending nitrogen separation tower bottom.
The utility model provides an among the complete liquefaction splitter of air-containing coal bed gas, preferably, the second cold box with be equipped with a pump on the pipeline between the entry of second gas-liquid separation jar for the liquid nitrogen that the pump sending obtained cools off in the second cold box.
The utility model provides an among the complete liquefaction splitter of air-containing coal bed gas, preferably, the export of the lower tower bottom of double-deck hydrocarbon oxygen knockout tower with be equipped with a pump between the second cold box for the liquefied natural gas that the pump sending obtained bottom the lower tower.
The utility model provides a contain full liquefaction splitter of air coal bed gas has following some advantages:
1. the double-layer hydrocarbon oxygen separation tower is adopted to replace a separate hydrocarbon separation tower and an oxygen separation tower, and meanwhile, a condenser evaporator is used to replace a reboiler and a recondenser, so that equipment can be reduced, and the process flow can be simplified; meanwhile, the condensation evaporator is adopted to combine the oxygen separation tower and the hydrocarbon separation tower, so that the cold and heat in the separation process can be fully utilized, and the cost is reduced;
2. through adopting the utility model provides a full liquefaction splitter can realize avoiding extravagant to the abundant separation of hydrocarbons, oxygen and nitrogen gas etc. in the coal bed gas that contains the air.
Drawings
The drawings are only intended to illustrate and explain the present invention and do not limit the scope of the invention. Wherein:
FIG. 1 is a schematic structural diagram of full liquefaction separation equipment for air-containing coal bed gas provided in example 1;
FIG. 2 is a schematic structural diagram of full liquefaction separation equipment for air-containing coal bed gas provided in example 2;
FIG. 3 is a schematic structural diagram of full liquefaction separation equipment for air-containing coal bed gas provided in example 3;
FIG. 4 is a schematic structural diagram of full liquefaction separation equipment for air-containing coal bed gas provided in example 4;
fig. 5 is the utility model provides a structural schematic diagram of the condensation evaporator of full liquefaction splitter.
The reference numbers illustrate:
a compression purification system 1; a cooling system, 2; a first stage compressor, 201; a first stage air cooler, 202; a first stage gas-liquid separation tank 203; a two-stage compressor, 204; a secondary air cooler 205; a second stage gas-liquid separation tank 206; a first cold box, 207; a second cold box, 208; a first JT valve, 209; a second JT valve, 210; feeding the tower 301; a lower tower 302; a condenser evaporator, 303; a nitrogen separation column, 304; a first gas-liquid separation tank, 305; a second knock out drum, 306; JT valve, 307; a pump, 308309310; a cooling device 4; a separator 401; an evaporation side inlet, 402; a condensation side outlet, 403; an evaporation side outlet, 404; condenser side inlet, 405.
Detailed Description
In order to understand the technical features, objects and advantages of the present invention more clearly, the following detailed description of the technical solution of the present invention is made with reference to the accompanying drawings, which are not intended to limit the implementable scope of the present invention.
Example 1
The embodiment provides full-liquefaction separation equipment for air-containing coal bed gas, and the structure of the full-liquefaction separation equipment is shown in figure 1.
The full liquefaction separation equipment comprises a compression purification system 1, a cooling system 2 and a liquefaction separation system, wherein the compression purification system 1 is used for compressing and purifying air-containing coal bed gas, the cooling system 2 is used for providing cold energy and cooling the air coal bed gas, and the compression purification system 1 and the cooling system both adopt systems commonly used in the field;
the liquefaction separation system comprises a double-layer hydrocarbon oxygen separation tower and a nitrogen separation tower 304, the double-layer hydrocarbon oxygen separation tower consists of an upper tower 301 and a lower tower 302, the middle part of the lower tower 302 is provided with an inlet for air-containing coal bed gas to enter, the bottom of the lower tower 302 is provided with an outlet for outputting liquefied natural gas, the top of the lower tower 302 is provided with an outlet, the top of the upper tower 301 is provided with a first inlet, a second inlet and an outlet, the bottom of the upper tower 301 is provided with an outlet for outputting liquid oxygen, and a condensation evaporator 303 is arranged between the upper tower 301 and the lower tower 302;
a pipeline for conveying the air-containing coal bed gas is connected to an inlet (an inlet for the air-containing coal bed gas to enter) in the middle of the lower tower 302 through the compression purification system 1 and the cooling system 2 in sequence;
the outlet at the top of the lower column 302 is connected to the first inlet at the top of the upper column 301 via JT valve 307;
an outlet at the top of the upper tower 301 is connected with an inlet at the bottom 304 of the nitrogen separation tower, an outlet at the top of the nitrogen separation tower 304 is a nitrogen outlet, and nitrogen can be cooled (the cooling can be realized by a conventional cooling device 4 or a cooling system 2) to obtain liquid nitrogen, wherein part of the nitrogen is output as a liquid nitrogen product and part of the nitrogen is used as reflux liquid;
an outlet at the bottom of the nitrogen separation column 304 is connected to a second inlet at the top of the upper column 301 through a pipe.
Example 2
The embodiment provides full-liquefaction separation equipment for air-containing coal bed gas, and the structure of the full-liquefaction separation equipment is shown in figure 2.
The full liquefaction separation equipment comprises a compression purification system 1, a cooling system 2 and a liquefaction separation system, wherein the compression purification system 1 is used for compressing and purifying air-containing coal bed gas, the cooling system 2 is used for providing cold energy, cooling the air coal bed gas and nitrogen output from the top of a nitrogen separation tower 304 and recovering the cold energy of partial products, and the two systems are commonly used in the field;
the liquefaction separation system comprises a double-layer hydrocarbon oxygen separation tower and a nitrogen separation tower 304, the double-layer hydrocarbon oxygen separation tower consists of an upper tower 301 and a lower tower 302, the middle part of the lower tower 302 is provided with an inlet for air-containing coal bed gas to enter, the bottom of the lower tower 302 is provided with an outlet for outputting liquefied natural gas, the top of the lower tower 302 is provided with an outlet, the top of the upper tower 301 is provided with a first inlet, a second inlet and an outlet, the bottom of the upper tower 301 is provided with an outlet for outputting liquid oxygen, and a condensation evaporator 303 is arranged between the upper tower 301 and the lower tower 302;
a pipeline for conveying the air-containing coal bed gas is connected to an inlet (an inlet for the air-containing coal bed gas to enter) in the middle of the lower tower 302 sequentially through the compression purification system 1 and the cooling system 2, an outlet (an outlet for outputting the liquefied natural gas) at the bottom of the lower tower 302 is connected with an inlet of the first gas-liquid separation tank 305 through the cooling system 2 through a pipeline, an outlet (a gas outlet) of the first gas-liquid separation tank 305 is connected with the inlet at the bottom of the lower tower 302 through a pipeline, and the first gas-liquid separation tank 305 is provided with an liquefied natural gas outlet (a liquid outlet);
the outlet at the top of the lower column 302 is connected to the first inlet at the top of the upper column 301 via JT valve 307;
an outlet at the top of the upper tower 301 is connected with an inlet at the bottom of the nitrogen separation tower 304, an outlet at the top of the nitrogen separation tower 304 is connected with a pipeline, the pipeline passes through the cooling system 2 to cool nitrogen in the pipeline, the pipeline is divided into two branches (branch pipelines) after passing through the cooling system 2, one branch is connected with a second inlet at the top of the nitrogen separation tower 304, and the other branch is used as a liquid nitrogen outlet and used for outputting a liquid nitrogen product;
the outlet at the bottom of the nitrogen separation column 304 is connected by a conduit to a second inlet at the top of the upper column 301, the upper column 301 having a liquid oxygen outlet at the bottom.
Example 3
The embodiment provides full liquefaction separation equipment for air-containing coal bed gas, wherein the adopted cooling system is an MRC device, and the structure of the MRC device is shown in FIG. 3.
In the full liquefaction separation equipment, the cooling system comprises a first-stage compressor 201, a first-stage air cooler 202, a first-stage gas-liquid separation tank 203, a second-stage compressor 204, a second-stage air cooler 205, a second-stage gas-liquid separation tank 206, a first cold box 207 and a second cold box 208, the first-stage gas-liquid separation tank 203 has an inlet, a top outlet and a bottom outlet, wherein:
a first-stage compressor 201, a first-stage air cooler 202, an inlet of a first-stage gas-liquid separation tank 203, a bottom outlet (liquid outlet) of the first-stage gas-liquid separation tank 203, a first cooling box (second flow passage) 207, a first JT valve 209 and a first cooling box (third flow passage) 207 are sequentially connected to form a high-temperature cycle;
a first-stage compressor 201, a first-stage air cooler 202, an inlet of a first-stage gas-liquid separation tank 203, a top outlet (gas outlet) of the first-stage gas-liquid separation tank 203, a second-stage compressor 204, a second-stage air cooler 205, a second-stage gas-liquid separation tank 206, a first cooling box (first flow passage) 207, a second cooling box (second flow passage) 208, a second JT valve 210, the second cooling box (third flow passage) 208 and the first cooling box (third flow passage) 207 are sequentially connected to form a low-temperature cycle;
a cryogenic pump 308 is arranged between the bottom outlet of the lower tower 302 of the double-layer hydrocarbon separation tower and the second cold box 208, and a pipeline for connecting the bottom outlet of the lower tower 302 and the first gas-liquid separation tank 305 passes through the second cold box (fifth flow channel) 208, so that cold and heat exchange between the low-temperature liquefied natural gas and the refrigerant is realized, and cold energy is recovered;
a cryogenic pump 309 is arranged between the bottom outlet of the nitrogen separation tower 304 and the second inlet at the top of the upper tower 302;
a pipe for connecting the top outlet of the nitrogen separation column 304 and the second gas-liquid separation tank 306 passes through the second cold box (first flow passage) 208, and is used for realizing cold-heat exchange between the cryogenic refrigerant and the nitrogen gas to prepare liquid nitrogen; a low-temperature pump 310 is arranged on a pipeline between the second cold box 208 and the second gas-liquid separation tank 306;
in the above-described total liquefaction separation apparatus, in the first cooling tank 207, four flow paths arranged in parallel from top to bottom are respectively a first flow path, a second flow path, a third flow path, and a fourth flow path, and in the second cooling tank 208, five flow paths arranged in parallel from top to bottom are respectively a first flow path, a second flow path, a third flow path, a fourth flow path, and a fifth flow path; the compressed and purified coal bed gas containing air sequentially passes through the fourth flow channel of the first cold box 207 and the fourth flow channel of the second cold box 208 for cooling, and then enters the lower tower 302.
The other structures of the full liquefaction separation device provided by the embodiment are the same as those of the embodiment 2.
The following takes the full liquefaction separation equipment of air-containing coal bed gas provided in embodiment 3 as an example, and the process (which is a process continuously performed) for performing full liquefaction separation of air-containing coal bed gas by using the equipment provided by the present invention is exemplified, but not limited thereto:
compressing and purifying the coal bed gas containing air by using a compression and purification system 1;
a pipeline for conveying compressed and purified air-containing coal bed gas (the molar content of methane, 49 percent, ethane, 1 percent, nitrogen, 40 percent, oxygen and 10 percent, the temperature is 30 ℃ and the pressure is 2000kPa) enters a first cold box 207, so that the air-containing coal bed gas exchanges heat with refrigerant, and the air-containing coal bed gas enters a lower tower 302 from an inlet at the middle part of the lower tower 302 of the double-layer hydrocarbon oxygen separation tower after being cooled to-145 ℃; the operating pressure of an upper tower 301 of the double-layer hydrocarbon oxygen separation tower is controlled to be 370kPa-400kPa, and the top of the upper tower 301 is connected with a nitrogen separation tower 304 through an external pipeline to form a complete rectification-stripping process;
the operating pressure in the lower tower 302 is controlled to be 885kPa-920kPa, the condensation temperature of the condensation evaporator 303 (the temperature at the top of the lower tower 302) is-167.1 ℃, and the cold energy provided by the reboiling of the liquid at the bottom of the upper tower 301 is utilized to cool and reflux (the gas at the top of the lower tower), so that clean air (mixed gas) with the temperature of-167.1 ℃ and the pressure of 885kPa is obtained at the top of the lower tower 302, wherein the molar content of methane is lower than 0.02 percent;
the liquid refluxed to the bottom of the lower column 302 has a temperature of-125.1 ℃ and a pressure of 920kPa, the main component of which is liquefied natural gas (pure hydrocarbons) which enters the second cold box 208 after passing through the cryopump 308 through the bottom outlet, the liquefied natural gas is subjected to heat exchange with the refrigerant in the second cold box 208 (the liquefied natural gas provides refrigeration and is itself heated), a part (for example, about 64.5%) of the liquefied natural gas is vaporized into gas, a mixture of gaseous and liquefied natural gas is formed, and then, the mixture enters the first gas-liquid separation tank 305 for separation, wherein the gaseous natural gas returns to the lower tower 302 through the gas outlet of the first gas-liquid separation tank 305 and flows upward, continues to participate in the liquefaction separation process, the liquefied natural gas is output from an outlet (liquid outlet) of the first gas-liquid separation tank 305, and becomes a high-purity Liquefied Natural Gas (LNG) product with a pressure of 920 kPa;
the mixed gas from which hydrocarbons are separated passes through an outlet at the top of the lower tower 302, is throttled to 410kPa by a JT valve 307, is cooled to-175.4 ℃, enters the upper tower 301, and enters the nitrogen separation tower 304 from the top of the upper tower 301;
in the nitrogen separation tower 304, gas flows from bottom to top, and in the flowing process, the gas and liquid flowing from top to bottom are subjected to heat and mass exchange, so that oxygen in the gas is gradually cooled into liquid and enters the liquid flowing from top to bottom, the liquid falls to the bottom of the nitrogen separation tower 304, nitrogen rises to the top, the nitrogen content is continuously increased and the oxygen content is continuously reduced along with the increase of the height, and the composition of the gas at the top of the nitrogen separation tower 304 (the temperature is-182.1 ℃, and the pressure is 380kPa) is close to that of pure nitrogen; the nitrogen enters a pipeline connected with an outlet at the top of the nitrogen separation tower 304, is cooled when passing through the second cold box 208, and is liquefied to obtain liquid nitrogen, and after passing through a second gas-liquid separation tank 306 (used for protecting a pump 310 under abnormal conditions) and the pump 310 in sequence, a part of the liquid nitrogen (for example, 70.6%) returns to the top of the nitrogen separation tower 304 to be used as reflux liquid for reflux, and the rest is output through an outlet to obtain a high-purity liquid nitrogen product, wherein the purity is over 99.98%; in the nitrogen separation column 304, the refluxed liquid is heat-mass exchanged with the gas flowing from bottom to top, and the nitrogen content is continuously decreased while the oxygen content is continuously increased (from top to bottom).
The liquid at the bottom of the nitrogen separation tower 304 enters the top of the upper tower 301 (enters through the second inlet) through the outlet at the bottom of the nitrogen separation tower 304, flows from top to bottom in the upper tower 301, and continuously performs heat and mass exchange with the gas flowing from bottom to top, so that liquid with a composition close to pure oxygen is obtained at the bottom of the upper tower; on the evaporation side (the side connected with the upper tower 301) of the condensation evaporator 303 at the bottom of the upper tower 301, the liquid is reboiled by utilizing the heat provided by the condensation reflux of the gas at the top of the lower tower 302 (the gas at the top of the lower tower 302 is condensed, and the gas is mainly composed of nitrogen and oxygen), so that the liquid (the composition is mainly composed of oxygen) in the gas is evaporated into the gas flowing from bottom to top and is subjected to heat and mass exchange with the liquid flowing from top to bottom, and the oxygen content in the gas is continuously reduced while the nitrogen content is continuously increased (from bottom to top). The part of the gas obtained by reboiling rises to the top of the upper column 301, is mixed with the gas entering the upper column 301 after throttling from the lower column, and then enters the bottom of the nitrogen separation column 304 together (the part of the gas enters the bottom of the nitrogen separation column 304 together with the mixed gas from the lower column 302 to participate in the separation in the nitrogen separation column 304), so that a high-purity liquid oxygen product containing a small amount of nitrogen (the molar content is less than 3%) and a very small amount of methane (the molar content is less than 0.1%) is obtained at the bottom of the upper column 301.
The liquid oxygen at the bottom of the upper tower 301 has lower temperature, and can provide cold for cooling the gas at the top of the lower tower 302 by the condensing evaporator 303, so that the heat exchange temperature difference can be reduced, the energy utilization efficiency is improved, equipment is reduced, the process flow is simplified, and the investment is reduced. In the above-described cold heat exchange, the reboiling temperature at the bottom of the upper column 302 (the temperature at the evaporation side of the condenser-evaporator 303) is-168.1 ℃ which is about 1 ℃ lower than the reflux temperature at the top of the lower column 302 (the condensation temperature, the temperature at the condensation side of the condenser-evaporator 303) of-167.1 ℃, and since both are connected by the condenser-evaporator 303 and exchange heat by phase change, the heat exchange temperature difference is small, and the energy utilization efficiency can be improved.
In the above-mentioned full liquefaction separation process, the refrigeration capacity is provided by a single-stage mixed refrigerant cycle device (MRC device), the content of nitrogen in the refrigerant (mixed refrigerant) is high to meet the refrigeration capacity requirement of the liquefaction separation system, and the molar composition of the refrigerant is as follows: 19.95% of methane, 12.37% of ethylene, 11.42% of propane, 10.46% of isopentane and 45.8% of nitrogen. The low-pressure mixed refrigerant is compressed to 1662kPa by a first-stage compressor 201, after being cooled to 40 ℃ in a first-stage air cooler 202, gas-liquid separation is carried out by a first-stage gas-liquid separation tank 203, the liquid-phase refrigerant is precooled to-80 ℃ by a first cooling tank 207, throttled to 260kPa by a JT valve 209 and then returned to the first cooling tank 207 for providing cold, the gas-phase refrigerant enters a second-stage compressor 204 and is compressed to 3988kPa, after being cooled to 40 ℃ in a second-stage air cooler 205, the gas-liquid two phases simultaneously pass through the first cooling tank 207 and a second cooling tank 208, after being cooled to-184 ℃, are throttled to 240kPa by a JT valve, the temperature is about-187 ℃, and then returned to the second cooling tank 208 for providing cold; the refrigerant is then heat exchanged with nitrogen from the top of the nitrogen separation column 304 in the second cold box to cool the nitrogen to liquid nitrogen, and also with liquid hydrocarbons from the bottom of the lower column 302 to recover cold and to cool the air-bearing coal seam gas after passing through the first cold box 207. The refrigerant from the second cooling tank 208 is mixed with the refrigerant from the J-T valve 209, and then the mixture is introduced into the first cooling tank 207 to provide cooling energy, so as to pre-cool the liquid refrigerant from the first-stage gas-liquid separation tank 203 and the refrigerant from the second-stage air cooler 205, and pre-cool the purified coal bed gas containing air.
Example 4
The embodiment provides full-liquefaction separation equipment for air-containing coal bed gas, and the structure of the full-liquefaction separation equipment is shown in figure 4. In the full liquefaction separation equipment, an inlet is arranged in the middle of a nitrogen separation tower 304, an outlet at the top of a lower tower 302 passes through a JT valve and the inlet in the middle of the nitrogen separation tower 304, a first inlet is not arranged at the top of an upper tower 301, and other basic structures are basically the same as those of the full liquefaction separation equipment adopted in the embodiment 3. In actual production, the heights of the double-layer hydrocarbon oxygen separation column and the nitrogen separation column 304 can be adjusted accordingly, the number of trays in the double-layer hydrocarbon oxygen separation column (upper column) is reduced, and the number of trays in the nitrogen separation column 304 is increased accordingly.
In the full liquefaction separation process using the full liquefaction separation equipment provided in this embodiment, the mixed gas from which hydrocarbons are separated in the lower column 302 passes through the outlet at the top of the lower column 302, is throttled to 410kPa by the JT valve 307, is cooled to-175.4 ℃, and then enters the upper column 301, but directly enters the inlet at the middle of the nitrogen separation column 304.
Example 5
This embodiment provides a condensing evaporator, which is a dipping bath type condensing evaporator integrally connected with upper and lower towers, and can adopt a single plate-fin type heat exchanger unit (i.e. condensing evaporator unit). The structure of the condensing evaporator is shown in fig. 5.
A single plate-fin type condensing evaporator unit is disposed at the center of the bottom of the upper tower, and the condensing evaporator is fixed to a partition 401 at the bottom of the upper tower by bolts (the partition divides the upper tower and the lower tower into two spaces which are not communicated with each other).
In actual operation, liquid oxygen will accumulate at the bottom of the upper column, thereby largely submerging the condensing evaporator unit in the liquid oxygen. The bottom of the condensing evaporator unit has an evaporation side inlet 402 and a condensation side outlet 403, and the top of the condensing evaporator unit has an evaporation side outlet 404 and a condensation side inlet 405. The evaporation side inlet 402 and the evaporation side outlet 404 of the condensing evaporator unit are connected to a flow channel in the condensing evaporator unit in which liquid oxygen is evaporated, and the condensation side inlet 405 and the condensation side outlet 403 of the condensing evaporator unit are connected to a flow channel in which the lower column top gas is condensed.
The gas at the top of the lower tower is connected with a condensing side inlet 405 at the top of the condensing evaporator through a pipeline, the gas at the top of the lower tower enters the condensing evaporator through the condensing side inlet 405 and then exchanges heat with liquid oxygen in the evaporator, so that part of gas from the lower tower is condensed into liquid and flows downwards, flows out from a condensing side outlet 403 at the bottom of the condensing evaporator and then flows back to the lower tower through a pipeline; the uncondensed gas from the lower tower is connected with a throttle valve through a pipeline (as shown in the rightmost side of the figure 5), and enters the upper tower after throttling or enters the middle part of the nitrogen separation tower after throttling.
Liquid oxygen enters the evaporation side of the condensation evaporator from an evaporation side inlet 402 at the bottom of the condensation evaporator, exchanges heat with gas from the lower tower, is gasified into gas and flows upwards, and flows out from an evaporation side outlet 404 at the top of the condensation evaporator to the large space of the upper tower. The evaporation side outlet and the evaporation side inlet can be communicated with the liquid accumulated at the bottom of the upper tower and the large space above the liquid, the size, the specific position and the shape of the opening of the evaporation side outlet and the evaporation side inlet are not required to be special, and the plate-fin condensation evaporator unit can be realized by removing the seal heads at the uppermost layer and the minimum layer of the evaporation side flow channel.
The embodiment provides only one in structure and the mode of setting of condensation evaporator, the utility model discloses what can adopt is not limited to this, and other condensation evaporators that can realize its function all can be used for the technical scheme of the utility model.
The above embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solutions of the present invention can be modified or equivalently replaced without departing from the spirit and scope of the technical solutions of the present invention.
Claims (10)
1. The utility model provides a full liquefaction splitter of coal bed gas that contains air, its includes compression clean system, cooling system and liquefaction piece-rate system, its characterized in that:
the liquefaction separation system comprises a double-layer hydrocarbon oxygen separation tower and a nitrogen separation tower, wherein the double-layer hydrocarbon oxygen separation tower consists of an upper tower and a lower tower, the lower tower is provided with an inlet for air-containing coal bed gas to enter, the bottom of the lower tower is provided with an outlet for outputting liquefied natural gas, the top of the lower tower is provided with an outlet, the top of the upper tower is provided with a second inlet and an outlet, the bottom of the upper tower is provided with an outlet for outputting liquid oxygen, and a condensation evaporator is arranged between the upper tower and the lower tower; the top of the nitrogen separation tower is provided with an outlet for outputting nitrogen, and the bottom of the nitrogen separation tower is provided with an inlet and an outlet; wherein,
a pipeline for conveying the coal bed gas containing air sequentially passes through the compression purification system and the cooling system and is connected to an inlet of the lower tower for the coal bed gas containing air to enter;
the top of the upper tower is provided with a first inlet, the outlet at the top of the lower tower is connected with the first inlet at the top of the upper tower through a JT valve, or the middle part of the nitrogen separation tower is provided with an inlet, and the outlet at the top of the lower tower is connected with the inlet at the middle part of the nitrogen separation tower through a JT valve;
an outlet at the top of the upper tower is connected with an inlet at the bottom of the nitrogen separation tower;
and an outlet at the bottom of the nitrogen separation tower is connected with a second inlet at the top of the upper tower.
2. The air-bearing coal seam gas full liquefaction separation equipment of claim 1, wherein the liquefaction separation system is provided with a first gas-liquid separation tank, the bottom of the lower tower is provided with an inlet, wherein an outlet at the bottom of the lower tower is connected with the inlet of the first gas-liquid separation tank through a pipeline, and the pipeline passes through the cooling system;
an outlet of the first gas-liquid separation tank is connected with an inlet at the bottom of the lower tower, and the first gas-liquid separation tank is also provided with an outlet for outputting liquefied natural gas.
3. The apparatus for full liquefaction separation of air-bearing coal seam gas according to claim 2, wherein the liquefaction separation system has a second gas-liquid separation tank, and wherein an outlet at the top of the nitrogen separation tower is connected to an inlet of the second gas-liquid separation tank after passing through the cooling system through a pipeline;
an outlet of the second gas-liquid separation tank is connected with a top inlet of the nitrogen separation tower, and the second gas-liquid separation tank is also provided with an outlet for outputting liquid nitrogen.
4. The air-bearing coal seam gas full liquefaction separation device of claim 3, wherein the cooling system comprises a primary compressor, a primary air cooler, a primary knockout drum, a secondary compressor, a secondary air cooler, a secondary knockout drum, a first cold box and a second cold box, the primary knockout drum having an inlet, a top outlet and a bottom outlet, wherein:
the first-section compressor, the first-section air cooler, the inlet of the first-section gas-liquid separation tank, the bottom outlet of the first-section separated gas-liquid tank, the first cold box, the first JT valve and the first cold box are sequentially connected to form high-temperature circulation;
the first-stage compressor, the first-stage air cooler, the inlet of the first-stage gas-liquid separation tank, the top outlet of the first-stage gas-liquid separation tank, the second-stage compressor, the second-stage air cooler, the second-stage gas-liquid separation tank, the first cooling box, the second JT valve, the second cooling box and the first cooling box are sequentially connected to form low-temperature circulation.
5. The full liquefaction separation equipment for air-bearing coal bed gas of claim 4, wherein a pipeline for conveying the air-bearing coal bed gas is connected to an inlet of the lower tower for the air-bearing coal bed gas to enter through the compression purification system, the first cold box and the second cold box in sequence.
6. The apparatus for full liquefaction separation of air-bearing coal seam gas according to claim 4, wherein the outlet at the top of the nitrogen separation tower is connected to the inlet of the second gas-liquid separation tank through a pipe and through the second cold box of the cooling system.
7. The full liquefaction separation equipment of air-bearing coal bed gas of claim 4, wherein the outlet at the bottom of the lower tower is connected with the inlet of the first gas-liquid separation tank through a pipeline and a second cold box of the cooling system.
8. The apparatus for full liquefaction separation of air-bearing coal seam gas of claim 1, wherein a pump is provided between the outlet at the bottom of the nitrogen separation column and the second inlet at the top of the upper column.
9. The apparatus for full liquefaction of air-bearing coal seam gas of claim 6, wherein a pump is provided in the conduit between the second cold box and the inlet of the second gas-liquid separation tank.
10. The apparatus for full liquefaction separation of air-bearing coal seam gas as claimed in claim 7, wherein a pump is provided between the outlet at the bottom of the lower tower of the double-layer hydrocarbon oxygen separation tower and the second cold box.
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| CN2010201717254U CN201688650U (en) | 2010-04-21 | 2010-04-21 | Full liquification separation equipment for coalbed gas containing air |
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| CN2010201717254U CN201688650U (en) | 2010-04-21 | 2010-04-21 | Full liquification separation equipment for coalbed gas containing air |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101818984A (en) * | 2010-04-21 | 2010-09-01 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
| CN102994184A (en) * | 2012-12-03 | 2013-03-27 | 中国石油集团工程设计有限责任公司 | Device and method for co-production of liquefied natural gas and liquid nitrogen |
| CN107917578A (en) * | 2017-11-13 | 2018-04-17 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
-
2010
- 2010-04-21 CN CN2010201717254U patent/CN201688650U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101818984A (en) * | 2010-04-21 | 2010-09-01 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
| CN102994184A (en) * | 2012-12-03 | 2013-03-27 | 中国石油集团工程设计有限责任公司 | Device and method for co-production of liquefied natural gas and liquid nitrogen |
| CN107917578A (en) * | 2017-11-13 | 2018-04-17 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
| CN107917578B (en) * | 2017-11-13 | 2019-10-25 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
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