CN201212765Y - Liquefaction separation device for chemical industrial exhaust - Google Patents
Liquefaction separation device for chemical industrial exhaust Download PDFInfo
- Publication number
- CN201212765Y CN201212765Y CNU2008201084663U CN200820108466U CN201212765Y CN 201212765 Y CN201212765 Y CN 201212765Y CN U2008201084663 U CNU2008201084663 U CN U2008201084663U CN 200820108466 U CN200820108466 U CN 200820108466U CN 201212765 Y CN201212765 Y CN 201212765Y
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- gas
- separation equipment
- heat exchanger
- fractionating column
- liquefaction separation
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Abstract
The utility model discloses a liquefying separation device for tail gas from the chemical industry, which comprises a second fractionating tower. A condenser and a gas outlet pipeline are arranged at the top of the fractionating tower, and an evaporator and a liquid product outlet pipeline are arranged at the bottom of the fractionating tower. The utility model can separate various constituents from the tail gas from the chemical industry, can more effectively utilize constituents contained in the tail gas from chemical industry, has simple device structure and low energy consumption, and is suitable for popularization.
Description
Technical field
The utility model relates to a kind of gas liquefaction separation equipment, the particularly a kind of chemical industry tail gas low-temperature liquefaction separation equipment that will be made up of mist.
Background technology
The tail gas that chemical engineering industry is produced is for example produced the tail gas of the coke-oven plant of coke, coal gas, the tail gas of coal-based artificial oil (or claiming the venting of speeding) etc., and it is relatively more complicated to be generally branch, is a kind of mist.For example have except that containing a large amount of hydrogen, also contain the above various alkane of carbon monoxide, nitrogen, methane, ethane, ethene, propane, propylene, butane and butane.These admixture of gas are that important resource but is difficult to well be utilized, and the method that existing employing transformation absorption or film separate all exists the rate of recovery low, the shortcoming that separation purity is not high.The Chinese invention patent of " a kind of separation liquefaction method and apparatus of mine gas gas of air backheating type " had once been proposed before the applicant, application number: 200810093653.3, this method and apparatus is mainly used in the separation of mine gas gas, equipment wherein includes only a fractionating column, can only separate and obtain a kind of fluid product, can't separate obtaining multiple available product, can not handle the chemical engineering industry tail gas that contains multiple gases.
Summary of the invention
Technical problem to be solved in the utility model provides a kind of liquefaction separation equipment of chemical industry tail gas, uses this equipment simultaneously the multiple composition in the chemical industry tail gas to be separated, and obtains multiple available product.Separation purity height, technology are simple, and energy consumption is also low.
For solving the problems of the technologies described above, chemical industry tail gas liquefaction separation equipment in the utility model, comprise the compression cleaning equipment, liquefaction separation equipment and refrigeration plant, the output pipe of the chemical industry tail gas unstripped gas of described compression cleaning equipment is connected with the raw material input channel of heat exchanger in the liquefaction separation equipment, described liquefaction separation equipment comprises the heat exchanger and first fractionating column, the unstripped gas output channel of described heat exchanger links to each other with the unstripped gas input port that is positioned at the fractionating column middle part, the refrigeration pipe of described refrigeration plant is connected with the refrigerating channel of liquefaction separation equipment heat exchanger, described liquefaction separation equipment also is provided with the after-fractionating tower, this fractionating column top has condenser, and its top also is provided with the gas introduction pipe simultaneously; This fractionating column bottom has evaporimeter, and its bottom also is provided with the liquid form product introduction pipe simultaneously, after-fractionating tower middle part the unstripped gas input port link to each other with the gas introduction pipe at the first fractionating column top.
As further improvement of the utility model, in this liquefaction separation equipment, the 3rd fractionating column is installed, the 3rd fractionating column top has condenser, and its top also is provided with the gas introduction pipe simultaneously; Fractionating column bottom has evaporimeter, and the bottom is provided with the liquid form product introduction pipe simultaneously, the 3rd fractionating column middle part the unstripped gas input port link to each other with the gas introduction pipe of after-fractionating top of tower.
Further, the gas introduction pipe of described after-fractionating top of tower with link to each other with the unstripped gas input port at the 3rd fractionating column middle part again after heat exchanger links to each other.
Further, the gas introduction pipe of described after-fractionating top of tower with cryogenic gas draw get back to heat exchanger after, be connected to decompressor, and then be connected to heat exchanger.
Further, the gas output tube road at described the 3rd fractionating column top links to each other with heat exchanger and reclaims cold.
Further, the gas introduction pipe at the described first fractionating column top with link to each other with the unstripped gas input port at after-fractionating tower middle part again after heat exchanger links to each other.
Further, the gas introduction pipe at the described first fractionating column top with cryogenic gas draw get back to heat exchanger after, be connected to decompressor, and then be connected to heat exchanger.
Further, the gas output tube road of described after-fractionating top of tower links to each other with heat exchanger and reclaims cold.
Further, the evaporimeter heating pipe line of described each fractionating column is connected with the precooling pipeline of refrigerant.
Further, the evaporimeter heating pipe line of described each fractionating column also can be connected with unstripped gas precooling pipeline.
Further, described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
Further, can comprise compressor and raw material gas purifying device in the described compression cleaning equipment; Described raw material gas purifying device can be the cleaning equipment of molecular sieve adsorption, also the cleaning system that can be made up of amine absorption tower and regenerator.
Described refrigeration plant can be a swell refrigeration, also can freeze with mix refrigerant, and also can be liquid nitrogen refrigerating.
The beneficial effects of the utility model are: the liquefaction separation equipment that adopts this chemical industry tail gas, can simultaneously the multiple gases composition that contains in the chemical industry tail gas be separated, can more effectively utilize the chemical industry tail gas that contains all gases, this device structure is simple simultaneously, energy consumption is low, helps applying.
Description of drawings
Fig. 1 is a kind of refrigeration plant of the present utility model and liquefaction separation equipment structural representation.
Fig. 2 is another kind of refrigeration plant of the present utility model and liquefaction separation equipment structural representation.
Fig. 3 is the structural representation of fractionating column in the utility model
The specific embodiment
Below in conjunction with accompanying drawing the utility model is described in further detail, institute gives an actual example and only is used to explain the utility model, is not to be used to limit scope of the present utility model.
Consult Fig. 1, be a kind of refrigeration plant of the present utility model and liquefaction separation equipment structural representation.
The liquefaction separation equipment comprises three grades of heat exchangers 1,2,3 and fractionating column 4,5; Condenser 6 is arranged at fractionating column 4 tops, and tower bottom has evaporimeter 7; Condenser 8 is arranged at fractionating column 5 tops, and tower bottom has evaporimeter 9; The refrigeration piping of condenser 6,8 links to each other with the pipeline of refrigeration system; The water back of evaporimeter 7 links to each other with the pipeline of hot nitrogen; The water back of evaporimeter 9 links to each other with the unstripped gas outlet conduit of heat exchanger 1; The unstripped gas pipeline links to each other with the water back of heat exchanger 1, evaporimeter 9 successively, and then is connected with fractionating column 4 middle parts; The gas pipeline at fractionating column 4 tops links to each other with the unstripped gas pipeline of heat exchanger 2,3 more successively; The fluid pipeline of fractionating column 4 bottoms is connected with liquid pump 10, storage tank 11 successively; The unstripped gas pipeline of heat exchanger 3 links to each other with the middle part of fractionating column 5 by pressure loading valve 12 again; Fractionating column 5 tops have gas pipeline to link to each other with heat exchanger 3,2,1 successively; Fractionating column 5 bottoms also have liquid line to link to each other with wet tank 13.
The refrigeration plant of the utility model embodiment 1 is a liquid nitrogen refrigerating system, has adopted a liquid nitrogen gas-liquid separator 14, air heater 15, heating agent heater 16.The fluid pipeline of liquid nitrogen gas-liquid separator 14 is connected with the refrigeration piping of condenser 8,6 successively; And then converge by the refrigeration feed channel of heat exchanger 2,1 and the gas pipeline of liquid nitrogen gas-liquid separator 14 successively, and be connected to air heater 15, heating agent heater 16 successively, be connected to the water back of evaporimeter 7; The water back of evaporimeter 7 is connected with the gas pipeline of heating agent heater 16 again; And then be connected to the regeneration gas pipeline of cleaning system; Cleaning system has adopted conventional molecular sieve adsorption system, here no longer narration.
The liquefying separation process step is as follows:
1, with chemical industry tail gas purification, dry carbon dioxide and the moisture removed;
2, the chemical industry tail gas after drying, the purification is fed heat exchanger 1, its temperature is cooled to about negative 40 degree Celsius;
3, the chemical industry tail gas after will lowering the temperature feeds evaporimeter 9 water backs of after-fractionating tower 5, and for it provides heat, gas temperature further is cooled to-60 ℃～-80 ℃ simultaneously, and a part is cooled to liquid in the gas;
4, more cooled chemical industry tail gas is fed the middle part of first fractionating column 4, 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 gases such as hydrogen, carbon monoxide, nitrogen, methane, ethene and a small amount of ethane at the top of fractionating column 4, the bottom of fractionating column 4 obtains most of ethane and propane, propylene, butane and above liquefied petroleum gas product.
5, liquefied petroleum gas product is pressed and delivered to storage in the storage tank 11 with pump 10.
6, will introduce the heat exchanger 2,3 from the isolated gas in first fractionating column, 4 tops, and continue to be cooled to below-160 ℃, after continuing to reduce through valve decompression temperature, feed the middle part of after-fractionating tower 5 again.
7, in after-fractionating tower 5, 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 gases such as hydrogen, carbon monoxide, nitrogen at the top of fractionating column 5, the bottom of fractionating column 5 obtains most liquid methane, and contains the low-temperature liquefaction natural gas liquids of a spot of ethane and very a spot of carbon monoxide.
8, the liquefied natural gas liquid product is transported to storage in the storage tank 13.
Needed cold is provided by liquid nitrogen refrigerating system in the above-mentioned liquefaction separation process, and the processing step of liquid nitrogen refrigerating system is as follows:
1, at first, liquid nitrogen enters liquid nitrogen gas-liquid separator 14 through pipeline, and liquid nitrogen steam comes out from the top of gas-liquid separator 14, enter air heater 15 heating, liquid nitrogen then comes out from the bottom of gas-liquid separator 14, passes through the refrigeration piping of condenser 8,6 successively, for condenser provides cold.
2, liquid nitrogen comes out from the refrigeration piping of condenser 8,6, has been evaporated to cold nitrogen, reclaims cold through heat exchanger 2,1 again, converges with the nitrogen that comes out in the top of gas-liquid separator 14 then, enters air heater 15 heating.
What 3, come out from air heater 15 is normal temperature nitrogen, enters heating agent heater 16 again and further heats, and temperature is elevated to 70 ℃ to 80 ℃, enters the evaporimeter 7 of first fractionating column 4 then, and for it provides heat, nitrogen temperature descends simultaneously.
4, nitrogen enters heating agent heater 16 again and further heats then, and temperature is elevated to 250 ℃, delivers to the molecular sieve tower of cleaning system, as regeneration gas.
Referring to Fig. 2, be another kind of refrigeration plant of the present utility model and liquefaction separation equipment structural representation.Basic identical among heat exchanger, fractionating column and the embodiment 1 of its liquefaction separating part, no longer repeat specification.Difference is that refrigeration system has adopted the method for mix refrigerant refrigeration, and mixed refrigerant systems 17 is ripe prior aries, does not need narration here.Just on equipment, the refrigerant pipeline of the condenser 6,8 of fractionating column is to be communicated with the refrigeration pipe of mix refrigerant refrigeration plant, rather than as embodiment 1, is connected with the liquid nitrogen pipeline.In addition, mixed refrigeration systems is a closed circulatory system, and cold-producing medium comes out to come back to refrigeration machine from heat exchanger.Therefore, the regeneration of the heating of evaporimeter 7 and molecular sieve needs to be heated afterwards through heater 16 by other gas in addition to realize.
Figure 3 shows that the structural representation of the described fractionating column of this utility model, the middle part of fractionating column is provided with mist and introduces pipeline 17 among the figure, and the top is provided with condenser 18, also is provided with gas introduction pipe 19 simultaneously, the bottom is provided with evaporimeter 20, also is provided with fluid product introduction pipe 21 simultaneously.
The above only is preferred embodiment of the present utility model, and is in order to restriction the utility model, not all within spirit of the present utility model and principle, any modification of being done, is equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (13)
1, a kind of chemical industry tail gas liquefaction separation equipment, comprise the compression cleaning equipment, liquefaction separation equipment and refrigeration plant, the output pipe of the chemical industry tail gas unstripped gas of described compression cleaning equipment is connected with the raw material input channel of heat exchanger in the liquefaction separation equipment, described liquefaction separation equipment comprises the heat exchanger and first fractionating column, the unstripped gas output channel of described heat exchanger links to each other with the unstripped gas input port that is positioned at first fractionating column middle part, the refrigeration pipe of described refrigeration plant is connected with the refrigerating channel of liquefaction separation equipment heat exchanger, it is characterized in that: described liquefaction separation equipment also is provided with the after-fractionating tower, this fractionating column top has condenser, and its top also is provided with the gas introduction pipe simultaneously; This fractionating column bottom has evaporimeter, and its bottom also is provided with the liquid form product introduction pipe simultaneously, and the gas introduction pipe at the first fractionating column top links to each other with the unstripped gas input port at after-fractionating tower middle part.
2, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 is characterized in that described liquefaction separation equipment also is provided with the 3rd fractionating column, and this fractionating column top has condenser, and its top also is provided with the gas introduction pipe simultaneously; This fractionating column bottom has evaporimeter, and its bottom also is provided with the liquid form product introduction pipe simultaneously, and the gas introduction pipe of after-fractionating top of tower links to each other with the unstripped gas input port at the 3rd fractionating column middle part.
3, a kind of chemical industry tail gas liquefaction separation equipment according to claim 2 is characterized in that, the gas introduction pipe of described after-fractionating top of tower with after heat exchanger links to each other again with the 3rd fractionating column in the middle part of the unstripped gas input port link to each other.
4, a kind of chemical industry tail gas liquefaction separation equipment according to claim 3 is characterized in that, the gas introduction pipe of described after-fractionating top of tower with cryogenic gas draw get back to heat exchanger after, be connected to decompressor, and then be connected to heat exchanger.
5, a kind of chemical industry tail gas liquefaction separation equipment according to claim 2 is characterized in that the gas output tube road at described the 3rd fractionating column top links to each other with heat exchanger and reclaims cold.
6, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 is characterized in that, the gas introduction pipe at the described first fractionating column top with after heat exchanger links to each other again with the after-fractionating tower in the middle part of the unstripped gas input port link to each other.
7, a kind of chemical industry tail gas liquefaction separation equipment according to claim 6 is characterized in that, the gas introduction pipe at the described first fractionating column top with cryogenic gas draw get back to heat exchanger after, be connected to decompressor, and then be connected to heat exchanger.
8, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 is characterized in that the gas output tube road of described after-fractionating top of tower links to each other with heat exchanger and reclaims cold.
9, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 and 2 is characterized in that the evaporimeter heating pipe line of described each fractionating column is connected with the precooling pipeline of refrigerant.
10, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 and 2, it is characterized in that, the unstripped gas pipeline of described compression cleaning equipment is connected with the raw gas heat medium channel of the heat exchanger of liquefaction in the separation equipment, and refrigeration plant is connected with the heat exchanger refrigerant passage of the separation equipment that liquefies.
11, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 and 2 is characterized in that described compression cleaning equipment comprises compressor and raw material gas purifying device; Described raw material gas purifying device is the cleaning equipment of molecular sieve adsorption, or the cleaning system of being made up of amine absorption tower and regenerator.
12, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 and 2 is characterized in that the refrigerant pipeline of the condenser of described each fractionating column and the refrigerant pipeline connection of heat exchanger; The liquid line of fractionating column bottom can insert the liquid in the liquid storage groove.
13, a kind of chemical industry tail gas liquefaction separation equipment according to claim 1 and 2 is characterized in that, described refrigeration plant can be nitrogen expansion refrigeration or nitrogen, methane swell refrigeration, also can freeze also available liquid nitrogen refrigerating with mix refrigerant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201084663U CN201212765Y (en) | 2008-06-05 | 2008-06-05 | Liquefaction separation device for chemical industrial exhaust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201084663U CN201212765Y (en) | 2008-06-05 | 2008-06-05 | Liquefaction separation device for chemical industrial exhaust |
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| Publication Number | Publication Date |
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| CN201212765Y true CN201212765Y (en) | 2009-03-25 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2008201084663U Expired - Lifetime CN201212765Y (en) | 2008-06-05 | 2008-06-05 | Liquefaction separation device for chemical industrial exhaust |
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| CN (1) | CN201212765Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101290184B (en) * | 2008-06-05 | 2010-10-13 | 北京国能时代能源科技发展有限公司 | Chemical industry tail gas liquefied separation method and equipment |
| CN101928617A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
-
2008
- 2008-06-05 CN CNU2008201084663U patent/CN201212765Y/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101290184B (en) * | 2008-06-05 | 2010-10-13 | 北京国能时代能源科技发展有限公司 | Chemical industry tail gas liquefied separation method and equipment |
| CN101928617A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
| CN101928617B (en) * | 2010-09-15 | 2013-03-20 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20090325 |