CN101493277B - Low temperature separation method and apparatus for mine gas - Google Patents
Low temperature separation method and apparatus for mine gas Download PDFInfo
- Publication number
- CN101493277B CN101493277B CN2009103004709A CN200910300470A CN101493277B CN 101493277 B CN101493277 B CN 101493277B CN 2009103004709 A CN2009103004709 A CN 2009103004709A CN 200910300470 A CN200910300470 A CN 200910300470A CN 101493277 B CN101493277 B CN 101493277B
- Authority
- CN
- China
- Prior art keywords
- gas
- heat exchanger
- fractionating column
- mine
- refrigeration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a mine gas low temperature separation method and equipment. The method comprises compressing and purifying the mine gas feed gas, removing the impurities in the feed gas to obtain compressed and purified mine gas; pumping the compressed and purified mine gas into a heat exchanger to lead the temperature to minus 82.5 DEG C; leading the cooled mine gas into the middle part of a fractionating tower, wherein the fractionating tower is provided with an evaporator at the bottom and a condenser at the top; obtaining low temperature air of high purity at the top of the fractionating tower and liquefied natural gas of high purity at the bottom of the fractionating tower; introducing the liquefied natural gas of high purity separated out from the fractionating tower into the heat exchanger as recovery of cold of refrigeration gas, and finally obtaining natural gas product of high purity in gas state, at the same time, introducing the low temperature air separated out from the top of the fractionating tower into the heat exchanger as recovery of cold of refrigeration gas. The method and equipment of the invention have simple structure, less energy consumption and low cost, and is favorable for promotion.
Description
Technical field
The present invention relates to a kind of gas separating method and equipment, particularly a kind of low temperature separating methods of mine gas gas and equipment.
Background technology
The coal bed gas of extraction is a mine gas gas in the coal mining process, because pressure is low, methane content is low, wherein is mixed with air, has brought difficulty for the processing and the transportation of this gas, all is that it is discharged in the atmosphere usually.This has not only caused serious atmosphere pollution, also causes the very big wasting of resources.If coal bed gas in this Device in Gas (mainly being methane) and air separation are come out, this will make transportation and utilize and all become very convenient.
Conventional separation method has absorption process, absorption method, film permeation method and cryogenic rectification method etc.The front several method, the purity of separation is difficult to reach requirement, and the rate of recovery that has is low, and what have also needs heating, and the Device in Gas that is mixed with air is explosive at high temperature, has potential safety hazard, does not therefore have and can be applied.A kind of technology has been invented by U.S. BCCK engineering company, be that the mine gas air pressure that will be mixed with air earlier contracts, with contact oxidation method wherein oxygen removed then, remove hydrogen sulfide and carbon dioxide then, remove moisture again, last method of separating with throttling refrigeration again removes nitrogen.This process equipment more complicated.The content that proposes in October, 2007 is in " air backheating type mine gas gas separates the liquefaction method and apparatus " Chinese patent application, (application number is: 200720178398.3) to have described a kind of cryogenic separation liquefaction process, this Processes and apparatus is simpler than the technology of U.S. BCCK, and can directly produce the methane of liquid.But, because its explained hereafter is the liquid natural gas product, therefore be suitable for remote conveying, and for the occasion that closely, only needs the gaseous natural gas product, just inapplicable.
Summary of the invention
Technical problem to be solved by this invention provides a kind of low temperature separating methods and equipment of mine gas gas, reclaim cold by adopting isolated liquid methane and making it turn back to heat exchanger, thereby can cut down the consumption of energy significantly, and produce natural gas product easy to use.
The technical scheme that the present invention solves the problems of the technologies described above is as follows: a kind of method of mine gas gas cryogenic separation, this method may further comprise the steps: step 1: the compression of mine gas unstripped gas is purified, remove the impurity in the unstripped gas, obtain compressing the mine gas gas of purification; Step 2: the mine gas gas of compressed purification enters cooled gas cooled in first heat exchanger, second heat exchanger, the 3rd heat exchanger and the 4th heat exchanger successively; Step 3: cooled mine gas gas enters the middle part of fractionating column, its liquid flows through column plate from top to bottom, the part of unstripped gas liquid is evaporated to gas in the evaporimeter of fractionating column bottom, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange; Step 4: upwards the gas that flows arrives the fractionating column top, and by the condenser condenses at fractionating column top, wherein a part is condensed into liquid again, refluxes downwards, carries out heat, matter exchange again with gas equally again; Step 5: the gas of emitting from the top of fractionating column is clean air, earlier reclaim a part of cold through the 4th heat exchanger, the 3rd heat exchanger and second heat exchanger, then, expand through decompressor again, enter the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the first heat exchanger backheat more successively, further reclaim cold; Step 6: what come out from the fractionating column bottom is exactly the very high liquefied natural gas of purity, this part liquid natural gas enters the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the gasification of first heat exchanger, backheat successively, reclaim cold, the natural gas of coming out from first heat exchanger can be sent to natural gas compressor, produces compressed natural gas.
The invention has the beneficial effects as follows: just can produce the natural gas product by adopting single fractionating column, have the advantage that manufacturing process is simple, cost is low, power consumption is little, especially be fit to closely utilize the occasion of coal mine mash gas.
On the basis of technique scheme, the present invention can also do following improvement.
Further, the chilling temperature of mine Device in Gas is-150 ℃ to-180 ℃ in the described step 2.
Further, cooled mine gas gas feeds the middle part of described fractionating column more earlier through after the pressure loading valve step-down in the described step 3.
Further, the evaporator evaporation temperature is-85 ℃ to-162 ℃ in the described step 3, and the condensation temperature of condenser is-150 ℃ to-200 ℃.
Further, in the described step 6, will feed the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and first heat exchanger more successively and reclaim cold from the isolated liquified natural gas in fractionating column bottom earlier through after the pressure loading valve step-down.
Further, in the described step 6, to from the isolated liquified natural gas in fractionating column bottom after reclaiming cold through the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and first heat exchanger and becoming the gaseous natural gas of normal temperature, become compressed natural gas by compressor compresses again.
Further, in the described step 6, to introduce the 4th heat exchanger successively from the isolated liquified natural gas in fractionating column bottom, the 3rd heat exchanger, when reclaiming cold as refrigerant in second heat exchanger and first heat exchanger, also comprise and to introduce the 4th heat exchanger successively from the isolated Cryogenic air in fractionating column top, the 3rd heat exchanger, reclaim cold as refrigeration gas in second heat exchanger and first heat exchanger, also can allow Cryogenic air earlier successively through the 4th heat exchanger, after the 3rd heat exchanger and second heat exchanger reclaim a part of cold, expand by decompressor again and lower the temperature, and then be connected to the 4th heat exchanger successively, the 3rd heat exchanger, second heat exchanger and first heat exchanger reclaim cold.
Further, the cold of described heat exchanger and condenser is provided by a refrigeration system, and described refrigeration system is gas swell refrigeration system or mix refrigerant refrigeration system.
Further, the refrigeration gas in the described refrigeration system can be earlier through the evaporimeter of fractionating column bottom, introduce again in the condenser at fractionating column top as refrigeration gas.
Further, refrigeration gas in the described refrigeration system is earlier through the evaporimeter of fractionating column bottom, gets back to the 3rd heat exchanger then further after the cooling, enters the condenser at fractionating column top again.
Further, with described from the isolated Cryogenic air in fractionating column top successively through after the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the first heat exchanger backheat, feed again cleaning equipment as the heating and swept-off gases.
The present invention also provides a kind of equipment that adopts above-mentioned mine gas gas cryogenic separation scheme for solving the problems of the technologies described above, and comprises compression cleaning equipment, refrigeration plant, separation equipment and auxiliary equipment; Described separation equipment comprises first heat exchanger, second heat exchanger, the 3rd heat exchanger, the 4th heat exchanger and a fractionating column, condenser is arranged at described fractionating column top, evaporimeter is arranged at the fractionating column bottom, the refrigeration piping of condenser links to each other with the refrigeration pipe of refrigeration plant, the water back of evaporimeter links to each other with the pipeline of refrigeration gas between first heat exchanger and the 3rd heat exchanger, the compression cleaning equipment the unstripped gas output pipe successively with first heat exchanger, second heat exchanger, the 3rd heat exchanger links to each other with the 4th heat exchanger, the unstripped gas outlet conduit of the 4th heat exchanger links to each other with the middle part of fractionating column, described fractionating column top have gas pipeline successively with the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger, decompressor, the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger links to each other with first heat exchanger, described fractionating column bottom also has liquid line that liquid natural gas is connected to the 4th heat exchanger successively by valve, the 3rd heat exchanger, second heat exchanger and first heat exchanger, be connected to auxiliary equipment then, described auxiliary equipment is the equipment of making nitrogen or natural gas compressor.
Described auxiliary equipment can be the equipment of making nitrogen.The equipment of making nitrogen can be varying-voltage adsorption nitrogen machine or preparing nitrogen by separating air machine, the nitrogen export pipeline of nitrogen making machine and the regeneration pipeline of cleaning equipment, also has the nitrogen pipeline of nitrogen refrigeration system to be connected.Auxiliary equipment can also have natural gas compressor, and the admission line of natural gas compressor is connected with the natural gas escape pipe of heat exchanger in the liquefaction separation equipment.
The invention has the beneficial effects as follows: only need a fractionating column, and do not need to build expensive liquefied natural gas storage tank, gas products is easy to use, and specific energy consumption is also low.
Further, be input to the temperature of unstripped gas of unstripped gas input port at fractionating column middle part below negative 82.5 degree Celsius.
Further, the unstripped gas output pipe of the 4th heat exchanger connects a pressure-reducing valve earlier, and then is connected to the input port at fractionating column middle part.
Further, the liquid output pipe road of fractionating column bottom connects a pressure-reducing valve earlier, and then is connected to the 4th heat exchanger.
Further, the evaporimeter heating pipe line of described fractionating column is connected with the unstripped gas pipeline.
Further, described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
Further, the cleaning equipment in the described compression cleaning equipment is the molecular sieve adsorption clarifier, or the cleaning system of being made up of amine absorption tower and regenerator.
Further, the inlet duct of the natural gas of described natural gas compressor is connected with the gas outlet pipeline of first heat exchanger.
The low temperature separating methods of mine gas gas of the present invention and equipment, utilized the coal mine mash gas resource of China's abundant, the Device in Gas that methane content is low is purified and is pure natural gas, and adopt the method for recycling the liquid cold, reduced energy consumption, reduced cost, the natural gas of producing more helps closely transporting and using.
Description of drawings
Fig. 1 is the schematic flow sheet of mine gas gas low temperature separating methods of the present invention;
Fig. 2 is the structural representation of compression cleaning equipment in the mine gas gas cryogenic separation of the present invention;
Fig. 3 is the schematic flow sheet of compression purification method in the mine gas gas low temperature separating methods of the present invention;
Fig. 4 is the structural representation of refrigeration plant in the mine gas gas cryogenic separation of the present invention and separation equipment first embodiment;
Fig. 5 is the schematic flow sheet of liquefied separation method first embodiment in the mine gas gas low temperature separating methods of the present invention;
Fig. 6 is the schematic flow sheet of refrigerating method first embodiment in the mine gas gas low temperature separating methods of the present invention;
Fig. 7 is the structural representation of refrigeration plant in the mine gas gas cryogenic separation of the present invention and separation equipment second embodiment;
Fig. 8 is the structural representation of fractionating column in the mine gas gas cryogenic separation of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing principle of the present invention and feature are described, institute gives an actual example and only is used to explain the present invention, is not to be used to limit scope of the present invention.
Fig. 1 is the schematic flow sheet of mine gas gas low temperature separating methods of the present invention.As shown in Figure 1, this method may further comprise the steps:
For example, the mine gas gas feeding heat exchanger that compression is purified carries out heat exchange, and its temperature is cooled to-150 ℃～-180 ℃, and most of mine gas gas is cooled to liquid.
Step 103, cooled mine gas gas fed the middle part of a fractionating column, evaporation and the condensation of evaporator overhead condenser, the gas and the liquid in the tower of the evaporimeter bottom fractionating column carry out sufficient matter, heat exchange, obtain highly purified Cryogenic air at the fractionating column top, the fractionating column bottom obtains highly purified liquified natural gas.
The present invention and application number are that 200610080889.4 first patent application is compared, this first patent application need be set up the two-stage fractionating column, and need mine gas gas is decomposed into nitrogen, oxygen-enriched air and liquified natural gas three parts, its technology is complicated, cost is also higher, production be fluid product.And the present invention adopts single fractionation column, production be gas products, and do not need from mine gas gas, to decomposite nitrogen and oxygen-enriched air, have the advantage that manufacturing process is simple, cost is low, power consumption is little, especially be fit to closely utilize the occasion of coal mine mash gas.
The present invention and application number are that 200610103425.0 second patent application is compared, though the single fractionation column structure has been adopted in this second patent application, but still need from mine gas gas, to decomposite nitrogen and oxygen-enriched air, a plurality of different temperature provinces need be set in fractionating column, and for separation of nitrogen needs also will provide lower temperature, so it still exists, and technology is complicated, the higher defective of cost; And equally also be to produce fluid product.By comparison, the present invention does not need to decomposite nitrogen and oxygen-enriched air from mine gas gas, production be gas products.Therefore, the present invention also obviously has the beneficial effect that technology is simple, cost is low, power consumption is little.
Fig. 2 is the structural representation of mine gas gas cryogenic separation compression cleaning equipment of the present invention.As shown in Figure 2, this compression cleaning equipment comprises filter 1, gas-liquid separator 2, compressor 3, cooler 4, gas-liquid separator 5, molecular sieve purification equipment group.Described molecular sieve purification equipment group comprises first molecular sieve drying machine 6 and second molecular sieve drying machine 7, and when first molecular sieve drying machine 6 work, second molecular sieve drying machine 7 thermal regeneration, cooling are standby, switch once in per 12 hours.This molecular sieve drying machine is mainly used to remove water and carbon dioxide.Described molecular sieve purification equipment group also is connected with filter 8 and heater 9.In addition, also have a varying-voltage adsorption nitrogen machine 10 that nitrogen is provided, be used for replacing the gas of compression cleaning equipment.This molecular sieve purification equipment is routine techniques, no longer describes in detail here.
Fig. 3 is compression purification method schematic flow sheet in the mine gas gas low temperature separating methods of the present invention.As shown in Figure 3, this method may further comprise the steps:
The mine gas gas unstripped gas that step 201, self-discharging pipeline come at first removes dust through filter 1.
After mine gas gas after step 202, the dedusting entered gas-liquid separator 2 gas-liquid separations, gas entered compressor 3 compressions.
Step 203, compression are after cooler 4 coolings are removed free water through gas-liquid separator 5 then.
Step 204, mine gas gas are introduced into first molecular sieve drying machine 6, deviate from water and carbon dioxide, behind the nitrogen that varying-voltage adsorption nitrogen machine 10 provides, enter second molecular sieve drying machine 7 again, displacement Device in Gas wherein, be heated to 240 ℃-250 ℃ with the pure air heater via 9 that produces in the flow process then, be used for the regeneration of second molecular sieve drying machine 7; After thermal regeneration is finished, pure air without heating, is directly imported second molecular sieve drying machine 7, the cooling molecular sieve, the temperature of second molecular sieve drying machine 7 of reduction, and then with the air in second molecular sieve drying machine 7 of nitrogen replacement, standby.
Step 205, the unstripped gas that removes water and carbon dioxide through the molecular sieve drying machine can enter refrigeration plant and separation equipment through filter 8 again.
Fig. 4 is the structural representation of refrigeration plant in the mine gas gas cryogenic separation of the present invention and separation equipment first embodiment.As shown in Figure 4, in the present embodiment, described separation equipment comprises level Four heat exchanger i.e. first heat exchanger 11, second heat exchanger 17, the 3rd heat exchanger 12, the 4th heat exchanger 13 and fractionating column 15.Condenser 16 is arranged at described fractionating column top, and evaporimeter 14 is arranged at the fractionating column bottom, and the refrigeration piping of condenser 16 links to each other with the pipeline of refrigeration gas, and the water back of evaporimeter 14 links to each other with the pipeline of refrigeration gas between first heat exchanger 11 and the 3rd heat exchanger 12.The unstripped gas pipeline links to each other with the 4th heat exchanger 13 with first heat exchanger 11, second heat exchanger 17, the 3rd heat exchanger 12 successively, and the unstripped gas outlet conduit of the 4th heat exchanger 13 links to each other with the middle part of fractionating column 15.Described fractionating column 15 tops have gas pipeline successively with the 4th heat exchanger 13, the 3rd heat exchanger 12 and second heat exchanger 17, decompressor 18, the four heat exchangers 13, the 3rd heat exchanger 12, second heat exchanger 17 link to each other with first heat exchanger 11.Described fractionating column 15 bottoms also have liquid line that liquid natural gas is connected to the 4th heat exchanger 13, the 3rd heat exchanger 12, second heat exchanger 17 and first heat exchanger 11 successively by valve, and being connected to auxiliary equipment then is natural gas compressor (natural gas compressor is expression in the drawings not).
Described refrigeration plant is the compression-expansion refrigeration system, has adopted the turbo-expander 23 of a compressor 19, cooler 20,22, band turbine supercharger 21.The refrigeration feed channel links to each other with the water back of evaporimeter 14 between first heat exchanger 11 and the 3rd heat exchanger 12, the gas exhaust piping of decompressor 23 links to each other with the refrigeration piping of condenser 16, links to each other with first heat exchanger 11 with the 4th heat exchanger 13, the 3rd heat exchanger 12, second heat exchanger 17 successively then.Described refrigeration plant can be nitrogen expansion refrigeration plant or nitrogen, methane swell refrigeration equipment, includes compressor, decompressor etc., also can use the mix refrigerant refrigeration plant, includes hybrid refrigeration compressor, cooler, gas-liquid separator etc.
Fig. 5 is the schematic flow sheet of liquefied separation method first embodiment in the mine gas gas low temperature separating methods of the present invention.As shown in Figure 5, this method may further comprise the steps:
The mine gas unstripped gas of step 301, compressed purification (methane 45%, air 55%) enters cooled gas cooled in first heat exchanger 11, second heat exchanger 17, the 3rd heat exchanger 12 and the 4th heat exchanger 13 successively, reduces temperature and reaches-175 ℃ approximately.
Unstripped gas after step 302, temperature descend enters the middle part of fractionating column 15, its liquid flows through column plate from top to bottom, the part of unstripped gas liquid is evaporated to gas in the evaporimeter 14 of fractionating column 15 bottoms, heating-up temperature is about-140 ℃, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange.
The 4th heat exchanger 13 in the above-mentioned liquefaction separation process, the 3rd heat exchanger 12, second heat exchanger 17, first heat exchanger 11 and condenser 16 needed colds are all provided by refrigeration system, described refrigeration plant comprises the compressor 19 that connects successively, cooler 20, turbine supercharger 21 and cooler 22, connect first heat exchanger 11 then, from first heat exchanger 11 come out further to connect the again pipeline of evaporimeter 14, refrigeration piping connects the 3rd heat exchanger 12 then, the refrigeration piping of the 3rd heat exchanger 12 is connected with the air inlet of turbo-expander 23 again, the exhaust outlet of turbo-expander 23 is connected with the refrigeration piping of condenser 16 again, connect the 4th heat exchanger 13 more successively, the 3rd heat exchanger 12, the cold medium channel of second heat exchanger 17 and first heat exchanger 11, at last, be connected to the inlet of compressor 19.Turbine supercharger 21 is driven by the rotating shaft of turbo-expander 23.
Fig. 6 is the schematic flow sheet of mine gas gas low temperature separating methods refrigerating method first embodiment of the present invention.As shown in Figure 6, this method may further comprise the steps:
Before step 401, refrigeration system start, be full of nitrogen in the system as refrigeration gas.
Step 402, the refrigeration system that starts, earlier compressed machine 19 compressions of refrigeration gas, 21 superchargings of turbine supercharger are passed through in cooling again in cooler 20, through cooler 22 coolings, enter 11 precoolings of first heat exchanger again, and temperature is reduced to-128 ℃.
Step 403, refrigeration gas are further cooled to-142 ℃ through the pipeline (temperature is for-143 ℃) of evaporimeter 14 again, and the gas that freezes then enters the 3rd heat exchanger 12, is further cooled to-150 ℃, enters turbo-expander 23 swell refrigerations again.
Fig. 7 is the structural representation of refrigeration plant in the mine gas gas cryogenic separation of the present invention and separation equipment second embodiment.As shown in Figure 7, in the present embodiment, the heat exchanger of described separation equipment, fractionating column and first embodiment are basic identical, in this no longer repeat specification.Difference is, makes unstripped gas be cooled to 0 ℃ to-50 ℃ by first heat exchanger 24 earlier, and the evaporimeter 27 of process fractionating column 28 bottoms is for evaporimeter provides heat then, and unstripped gas itself obtains precooling simultaneously.Therefore, on equipment, the heating pipe line of the evaporimeter 27 of fractionating column 28 is connected with the unstripped gas pipeline, and unstripped gas is cooled to-150 ℃～-180 ℃ through the 3rd heat exchanger 25 and the 4th heat exchanger 26 more then, make most of mine gas gas be cooled to liquid, enter the middle part of fractionating column 28 again.Difference is more in addition, refrigeration system has adopted the method for mix refrigerant refrigeration, mixed refrigerant systems is by mix refrigerant compressor assembly 32,35, aftercooler 33,36, gas-liquid separator 34,37 and several throttle are formed, this is ripe prior art, does not need narration here.Just on equipment, the refrigerant pipeline of the condenser 29 of fractionating column is to be communicated with the refrigeration pipe of mix refrigerant refrigeration plant, is different among first embodiment to be connected with the expander refrigeration air pipe of nitrogen refrigeration.
Fig. 8 is the structural representation of fractionating column in the mine gas gas cryogenic separation of the present invention.As shown in Figure 8, simultaneously referring to Fig. 4, the top of described fractionating column 15 is provided with condenser 16, and the bottom of fractionating column 15 is provided with evaporimeter 14.The structure of the fractionating column 15 among the fractionating column 28 among second embodiment and first embodiment is identical.
Mine gas gas cryogenic separation among the present invention and application number are that 200720178398.3 patent application is compared, and the present invention does not need to build expensive liquefied natural gas storage tank, and gas products is easy to use, and specific energy consumption is also low.
The above only is preferred embodiment of the present invention, and is in order to restriction the present invention, within the spirit and principles in the present invention not all, any modification of being done, is equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (19)
1. the method for a mine gas gas cryogenic separation, it is characterized in that: this method may further comprise the steps:
Step 1: the compression of mine gas unstripped gas is purified, remove the impurity in the unstripped gas, obtain compressing the mine gas gas of purification;
Step 2: the mine gas gas of compressed purification enters cooled gas cooled in first heat exchanger, second heat exchanger, the 3rd heat exchanger and the 4th heat exchanger successively;
Step 3: cooled mine gas gas enters the middle part of fractionating column, its liquid flows through column plate from top to bottom, the part of unstripped gas liquid is evaporated to gas in the evaporimeter of fractionating column bottom, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange;
Step 4: upwards the gas that flows arrives the fractionating column top, and by the condenser condenses at fractionating column top, wherein a part is condensed into liquid again, refluxes downwards, carries out heat, matter exchange again with gas equally again;
Step 5: the gas of emitting from the top of fractionating column is clean air, earlier reclaim a part of cold through the 4th heat exchanger, the 3rd heat exchanger and second heat exchanger, then, expand through decompressor again, enter the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the first heat exchanger backheat more successively, further reclaim cold;
Step 6: what come out from the fractionating column bottom is exactly the very high liquefied natural gas of purity, this part liquid natural gas enters the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the gasification of first heat exchanger, backheat successively, reclaim cold, the natural gas of coming out from first heat exchanger can be sent to natural gas compressor, produces compressed natural gas.
2. the method for mine gas gas cryogenic separation according to claim 1 is characterized in that: the chilling temperature of mine Device in Gas is-150 ℃ to-180 ℃ in the described step 2.
3. the method for mine gas gas cryogenic separation according to claim 1 is characterized in that: cooled mine gas gas feeds the middle part of described fractionating column more earlier through after the pressure loading valve step-down in the described step 3.
4. the method for mine gas gas cryogenic separation according to claim 1 is characterized in that: the evaporator evaporation temperature is-85 ℃ to-162 ℃ in the described step 3, and the condensation temperature of condenser is-150 ℃ to-200 ℃ in the described step 4.
5. the method for mine gas gas cryogenic separation according to claim 1, it is characterized in that: in the described step 6, to feed the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and first heat exchanger more successively and reclaim cold from the isolated liquified natural gas in fractionating column bottom earlier through after the pressure loading valve step-down.
6. the method for mine gas gas cryogenic separation according to claim 1, it is characterized in that: in the described step 6, to from the isolated liquified natural gas in fractionating column bottom after reclaiming cold successively through the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and first heat exchanger and becoming the gaseous natural gas of normal temperature, become compressed natural gas by compressor compresses again.
7. the method for mine gas gas cryogenic separation according to claim 1, it is characterized in that: in the described step 6, to introduce the 4th heat exchanger successively from the isolated liquified natural gas in fractionating column bottom, the 3rd heat exchanger, when reclaiming cold as refrigerant in second heat exchanger and first heat exchanger, also comprise and to introduce the 4th heat exchanger successively from the isolated Cryogenic air in fractionating column top, reclaim cold as refrigeration gas in the 3rd heat exchanger and second heat exchanger, allow Cryogenic air earlier successively through the 4th heat exchanger, after the 3rd heat exchanger and second heat exchanger reclaim a part of cold, expand by decompressor again and lower the temperature, and then be connected to the 4th heat exchanger successively, the 3rd heat exchanger, second heat exchanger and first heat exchanger reclaim cold.
8. according to the method for the arbitrary described mine gas gas cryogenic separation of claim 1-7, it is characterized in that: the cold of described heat exchanger and condenser is provided by a refrigeration system, and described refrigeration system is gas swell refrigeration system or mix refrigerant refrigeration system.
9. the method for mine gas gas cryogenic separation according to claim 8 is characterized in that: refrigeration gas in the described refrigeration system is earlier through the evaporimeter of fractionating column bottom, introduces in the condenser at fractionating column top as refrigeration gas again.
10. the method for mine gas gas cryogenic separation according to claim 8, it is characterized in that: the refrigeration gas in the described refrigeration system is the evaporimeter of process fractionating column bottom earlier, after getting back to the further cooling of the 3rd heat exchanger then, enter the condenser at fractionating column top again.
11. the method for mine gas gas cryogenic separation according to claim 1, it is characterized in that: reclaim a part of cold through the 4th heat exchanger, the 3rd heat exchanger and second heat exchanger successively from the isolated Cryogenic air in fractionating column top described, then, expand through decompressor again, after entering the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger and the first heat exchanger backheat more successively, feed cleaning equipment again as heating and swept-off gases.
12. a mine gas gas cryogenic separation comprises compression cleaning equipment, refrigeration plant, separation equipment and auxiliary equipment;
Described separation equipment comprises first heat exchanger, second heat exchanger, the 3rd heat exchanger, the 4th heat exchanger and a fractionating column, condenser is arranged at described fractionating column top, evaporimeter is arranged at the fractionating column bottom, the refrigeration piping of condenser links to each other with the refrigeration pipe of refrigeration plant, the water back of evaporimeter links to each other with the pipeline of refrigeration gas between first heat exchanger and the 3rd heat exchanger, the compression cleaning equipment the unstripped gas output pipe successively with first heat exchanger, second heat exchanger, the 3rd heat exchanger links to each other with the 4th heat exchanger, the unstripped gas outlet conduit of the 4th heat exchanger links to each other with the middle part of fractionating column, described fractionating column top have gas pipeline successively with the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger, decompressor, the 4th heat exchanger, the 3rd heat exchanger, second heat exchanger links to each other with first heat exchanger, described fractionating column bottom also has liquid line that liquid natural gas is connected to the 4th heat exchanger successively by valve, the 3rd heat exchanger, second heat exchanger and first heat exchanger, be connected to auxiliary equipment then, described auxiliary equipment is the equipment of making nitrogen or natural gas compressor.
13. mine gas gas cryogenic separation according to claim 12 is characterized in that: the temperature of unstripped gas of unstripped gas input port that is input to fractionating column middle part is below negative 82.5 degree Celsius.
14. mine gas gas cryogenic separation according to claim 12 is characterized in that: the unstripped gas output pipe of the 4th heat exchanger connects a pressure-reducing valve earlier, and then is connected to the input port at fractionating column middle part.
15. mine gas gas cryogenic separation according to claim 12 is characterized in that: the liquid output pipe road of fractionating column bottom connects a pressure-reducing valve earlier, and then is connected to the 4th heat exchanger.
16. according to the arbitrary described mine gas gas cryogenic separation of claim 13-15, it is characterized in that: the evaporimeter heating pipe line of described fractionating column is connected with the unstripped gas pipeline.
17. according to the arbitrary described mine gas gas cryogenic separation of claim 13-15, it is characterized in that: described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
18. according to the arbitrary described mine gas gas cryogenic separation of claim 13-15, it is characterized in that: the cleaning equipment in the described compression cleaning equipment is the molecular sieve adsorption clarifier, or the cleaning system of being made up of amine absorption tower and regenerator.
19. mine gas gas cryogenic separation according to claim 12 is characterized in that: when described auxiliary equipment was natural gas compressor, the inlet duct of the natural gas of described natural gas compressor was connected with the gas outlet pipeline of first heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009103004709A CN101493277B (en) | 2009-02-18 | 2009-02-18 | Low temperature separation method and apparatus for mine gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009103004709A CN101493277B (en) | 2009-02-18 | 2009-02-18 | Low temperature separation method and apparatus for mine gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101493277A CN101493277A (en) | 2009-07-29 |
| CN101493277B true CN101493277B (en) | 2011-10-05 |
Family
ID=40923989
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009103004709A Expired - Fee Related CN101493277B (en) | 2009-02-18 | 2009-02-18 | Low temperature separation method and apparatus for mine gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101493277B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103773529B (en) * | 2012-10-24 | 2015-05-13 | 中国石油化工股份有限公司 | Pry-mounted associated gas liquefaction system |
| CN103146450B (en) * | 2013-03-29 | 2014-05-21 | 四川金科深冷设备工程有限公司 | Natural gas recovery process |
| CN108318621B (en) * | 2018-01-05 | 2021-02-12 | 南通仁隆科研仪器有限公司 | Coal bed gas detection equipment with explosion-proof and gas collection function |
-
2009
- 2009-02-18 CN CN2009103004709A patent/CN101493277B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN101493277A (en) | 2009-07-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201199120Y (en) | Separated liquefaction equipment of air conditioner back heating type mine gas | |
| CN109838975B (en) | Low-energy-consumption liquid nitrogen preparation device and process | |
| CN100404988C (en) | Air-contained coal gas gasification and separation process and equipment | |
| CN108061428B (en) | Pure nitrogen preparation device and process | |
| CN103123203B (en) | Method of preparing pure nitrogen by using exhaust gas with nitrogen to carry out once-more cryogenic distillation | |
| CN103523751B (en) | Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen | |
| CN115069057B (en) | Method for purifying and recovering carbon dioxide by low-temperature rectification | |
| CN105716370A (en) | System and method of preparing hydrogen rich gas and carbon monoxide from synthesis gas | |
| CN104807290A (en) | Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion | |
| AU2010291532B2 (en) | Method and device for treating a carbon dioxide-containing gas flow, wherein the energy of the vent gas (work and cold due to expansion) is used | |
| CN1952569A (en) | Process and equipment for liquefying air-containing coal-bed gas | |
| CN202204239U (en) | Device for producing high-purity nitrogen and low-purity oxygen with pressure | |
| CN200952872Y (en) | Air-containing coal seam gas liquifying separating equipment | |
| CN101493277B (en) | Low temperature separation method and apparatus for mine gas | |
| CN107641535B (en) | Device and method for separating and purifying various gases by membrane cryogenic coupling | |
| CN207365553U (en) | A kind of device for producing high pure oxygen and High Purity Nitrogen | |
| CN101509722A (en) | Distillation method and apparatus | |
| CN115790076B (en) | Device and method for recycling carbon dioxide and nitrogen in flue gas | |
| CN201359420Y (en) | Low temperature separation equipment of mine gas | |
| CN2898737Y (en) | Liquefier containing coal-seam gas | |
| CN109357475B (en) | System for cascade utilization LNG cold energy prepares liquid oxygen liquid nitrogen | |
| CN114165987B (en) | Liquid carbon dioxide production device and production method thereof | |
| CN200979332Y (en) | Air-containing coal layer gas-liquid separation apparatus | |
| CN114440553A (en) | Low-energy-consumption double-tower pure nitrogen preparation device adopting nitrogen expansion refrigeration and application method | |
| CN1118060A (en) | Method for extracting high-pure helium from natural gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111005 Termination date: 20180218 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |