CN208990490U - A kind of device of off-gas recovery dry ice - Google Patents
A kind of device of off-gas recovery dry ice Download PDFInfo
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- CN208990490U CN208990490U CN201821697278.9U CN201821697278U CN208990490U CN 208990490 U CN208990490 U CN 208990490U CN 201821697278 U CN201821697278 U CN 201821697278U CN 208990490 U CN208990490 U CN 208990490U
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Abstract
The utility model discloses a kind of devices of off-gas recovery dry ice, including air-introduced machine, power plant FGD exiting flue gas pipeline, water cooling heat exchanger, the first gas-liquid separator, low temperature dehumidification device, the second gas-liquid separator, molecular sieve dehumidifier, cold recovery exchanger, cold washing tower, smoke exhaust system, solid-liquid separator, subcolling condenser, circulation and water cooler, the device can be recycled the carbon dioxide in flue gas in the form of dry ice, and economy is higher.
Description
Technical field
The utility model belongs to flue gas decarbonization and dry ice manufacture technology field, is related to a kind of device of off-gas recovery dry ice.
Background technique
Dry ice is solid carbon dioxide.The three phase point of carbon dioxide is (- 57 DEG C, 527kPa).When pressure is lower than
When 527kPa, dry ice is directly sublimated into gaseous carbon dioxide cooling；When pressure is higher than 527kPa, gaseous carbon dioxide cooling is cold
Liquid carbon dioxide is congealed into, continues cooling and then becomes dry ice.The application of dry ice is very extensive, can be used for rain making, food is protected
The multiple fields such as fresh, Dry ice cleaning, stage effect.The method of industrial production dry ice generally first passes through in the case where pressurization at present
Liquid carbon dioxide is obtained, then so that operative liquid carbon dioxide is solidified as solid-state powder using liquid carbon dioxide evaporative cooling
End, by hydraulic press device, dry ice powder is squeezed into particle, column, sheet, that block-like dry ice of various shapes；About
40% liquid carbon dioxide switchs to solid dry ice.
Contain a large amount of carbon dioxide gas in the flue gas that fire coal generates.It is industrial at present generally by chemical absorption method or
Pressure swing adsorption method isolates the carbon dioxide in flue gas, and liquid carbon dioxide product then is made by the techniques such as compressing and liquefying.
Due to the higher cost of flue gas decarbonization, the market price of liquid carbon dioxide product is lower, therefore titanium dioxide is trapped from flue gas
The economy that carbon produces liquid carbon dioxide technique is not high, so that the large-scale commercial for also constraining flue gas carbon capture technology pushes away
Extensively.
Utility model content
The shortcomings that the purpose of the utility model is to overcome the above-mentioned prior arts provides a kind of dress of off-gas recovery dry ice
It sets, which can be recycled the carbon dioxide in flue gas in the form of dry ice, and economy is higher.
In order to achieve the above objectives, the device of off-gas recovery dry ice described in the utility model includes that air-introduced machine, power plant FGD go out
Mouthful flue, water cooling heat exchanger, the first gas-liquid separator, low temperature dehumidification device, the second gas-liquid separator, molecular sieve dehumidifier,
Cold recovery exchanger, cold washing tower, smoke exhaust system, solid-liquid separator, subcolling condenser, circulation and cold water
Unit；
The entrance of air-introduced machine is connected with power plant FGD exiting flue gas pipeline, the heat of the water cooled heat exchanger in outlet of air-introduced machine
Side is connected with the entrance of the first gas-liquid separator, and the gas side of the first gas-liquid separator exports hot side through low temperature dehumidification device and the
The entrance of two gas-liquid separators is connected, and the gas side outlet of the second gas-liquid separator is connected with the entrance of molecular sieve dehumidifier,
Hot side of the outlet of molecular sieve dehumidifier through cold recovery exchanger is connected with the gas access of cold washing tower bottom, low temperature
Exhanst gas outlet at the top of scrubbing tower is connected with the cold side input port of cold recovery exchanger, the cold side outlet port of cold recovery exchanger
It is connected with smoke exhaust system, the serum outlet of cold washing tower bottom is connected with the entrance of solid-liquid separator, solid-liquid point
Liquid outlet from device is connected with the hot side entrance of subcolling condenser, in the hot side outlet and cold washing tower of subcolling condenser
The liquid inlet at end is connected；
The cold side of water cooling heat exchanger is connected with circulation, and the cold side of low temperature dehumidification device is connected with water cooler,
The cold side of subcolling condenser is connected with Cryo Refrigerator.
It further include header tank, the discharge outlet of the first gas-liquid separator, the discharge outlet of the second gas-liquid separator and molecule screen out
The discharge outlet of wet device is connected with the entrance of header tank.
The serum outlet of cold washing tower bottom is pumped through low temperature slurries to be connected with solid-liquid separator entrance.
The liquid outlet of solid-liquid separator is pumped through low-temperature circulating to be connected with the heat survey entrance of subcolling condenser.
It further include refrigerant replenishment system and dry ice molding machine, wherein refrigerant inlet and refrigerant the supplement system of solid-liquid separator
System is connected, and the solid outlet of solid-liquid separator is connected with dry ice molding machine.
The utility model has the following beneficial effects:
The device of off-gas recovery dry ice described in the utility model is removed when specific operation using water cooling heat exchanger, low temperature
Wet device, cold recovery exchanger and cold washing tower cool down flue gas, so that the carbon dioxide in flue gas forms dry ice, so
Dry ice is isolated by solid-liquid separator afterwards, to realize the recycling of dry ice.In addition, the utility model passes through the first gas-liquid separation
Device, the second gas-liquid separator, low temperature dehumidification device and molecular sieve dehumidifier remove the water in flue gas, to improve the purity of dry ice, together
When avoid influence of the water to subsequent processing in flue gas.To prevent the drikold for sublimating out to be attached to flue gas condenser table
Face simultaneously blocks condenser, and the utility model carries out direct contact type cooling to flue gas using cryogenic freezing liquid, and that sublimates out is dry
Ice flows out in solid-liquid separator with freezing liquid, then isolates solid dry ice by solid-liquid separator, to realize returning for dry ice
It receives, compared to the liquid carbon dioxide that conventional carbon dioxide trapping system obtains, value of the product is high.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the utility model.
Wherein, 1 it is air-introduced machine, 2 be water cooling heat exchanger, 3 be circulation, 4 be the first gas-liquid separator, 5 is low temperature
Dehumidifier, 6 be water cooler, 7 be gas-liquid separator, 8 be molecular sieve dehumidifier, 9 be header tank, 10 be cold recovery exchange
Device, 11 be cold washing tower, 12 be low temperature slurries pump, 13 be solid-liquid separator, 14 be low-temperature circulating pump, 15 be sub-cooled
Device, 16 be Cryo Refrigerator, 17 be dry ice molding machine, 18 be refrigerant replenishment system.
Specific embodiment
The utility model is described in further detail with reference to the accompanying drawing:
With reference to Fig. 1, the device of off-gas recovery dry ice described in the utility model includes air-introduced machine 1, power plant's FGD exiting flue gas
It is pipeline, water cooling heat exchanger 2, the first gas-liquid separator 4, low temperature dehumidification device 5, the second gas-liquid separator 7, molecular sieve dehumidifier 8, cold
Amount recycling heat exchanger 10, cold washing tower 11, smoke exhaust system, solid-liquid separator 13, subcolling condenser 15, circulation
3 and water cooler 6；The entrance of air-introduced machine 1 is connected with power plant FGD exiting flue gas pipeline, the water cooled heat exchange in the outlet of air-introduced machine 1
The hot side of device 2 is connected with the entrance of the first gas-liquid separator 4, and the gas side of the first gas-liquid separator 4 is exported through low temperature dehumidification device 5
Hot side be connected with the entrance of the second gas-liquid separator 7, the outlet of the gas side of the second gas-liquid separator 7 and molecular sieve dehumidifier 8
Entrance be connected, the outlet of molecular sieve dehumidifier 8 is through the hot side of cold recovery exchanger 10 and 11 bottom of cold washing tower
Gas access is connected, and the exhanst gas outlet at 11 top of cold washing tower is connected with the cold side input port of cold recovery exchanger 10,
The cold side outlet port of cold recovery exchanger 10 is connected with smoke exhaust system, the serum outlet of 11 bottom of cold washing tower and solid
The entrance of liquid/gas separator 13 is connected, and the liquid outlet of solid-liquid separator 13 is connected with the hot side entrance of subcolling condenser 15,
The hot side outlet of subcolling condenser 15 is connected with the liquid inlet of 11 upper end of cold washing tower；The cold side of water cooling heat exchanger 2 with
Circulation 3 is connected, and the cold side of low temperature dehumidification device 5 is connected with water cooler 6, the cold side of subcolling condenser 15 and low temperature
Refrigeration machine 16 is connected.The utility model further includes header tank 9, the discharge outlet of the first gas-liquid separator 4, the second gas-liquid separator
7 discharge outlet and the discharge outlet of molecular sieve dehumidifier 8 are connected with the entrance of header tank 9.
Specifically, the serum outlet of 11 bottom of cold washing tower is through low temperature slurries pump 12 and 13 entrance phase of solid-liquid separator
Even；The liquid outlet of solid-liquid separator 13 surveys entrance with the heat of subcolling condenser 15 through low-temperature circulating pump 14 and is connected.
The utility model further includes refrigerant replenishment system 18 and dry ice molding machine 17, wherein the refrigerant of solid-liquid separator 13
Entrance is connected with refrigerant replenishment system 18, and the solid outlet of solid-liquid separator 13 is connected with dry ice molding machine 17.
The specific work process of the utility model are as follows:
Flue gas after FGD desulfurization, which is entered by air-introduced machine 1 in the hot side of water cooling heat exchanger 2, is cooled to 35 DEG C, then through the
One gas-liquid separator 4 carries out gas-liquid separation, wherein the gas that the first gas-liquid separator 4 is isolated dehumidifies through low temperature dehumidification device 5 to drop
Temperature carries out gas-liquid separation to entering in the second gas-liquid separator 7 after 2 DEG C, the gas that the second gas-liquid separator 7 is isolated through point
Son sieve dehumidifier 8 dehumidifying and 10 hot side of cold recovery exchanger enter in cold washing tower 11 after being cooled to -68 DEG C；
In cold washing tower 11, -110 DEG C of low temperature normal propyl alcohols that flue gas is got off by 11 top spray of cold washing tower are cooling
To -105 DEG C, to isolate dry ice, wherein -105 DEG C of flue gases exported at the top of cold washing tower 11 enter cold recovery exchange
Heat absorption is to -20 DEG C in the cold side of device 10, and then into smoke exhaust system, dry ice and low temperature in cold washing tower 11 are just
Propyl alcohol is mixed to form -90 DEG C of low temperature slurries, -90 DEG C of low temperature slurries through the serum outlet of 11 bottom of cold washing tower export to
It is separated by solid-liquid separation in solid-liquid separator 13, wherein the dry ice that solid-liquid separator 13 is isolated is expelled directly out, to realize in flue gas
The recycling of dry ice, the liquid that solid-liquid separator 13 is isolated are washed after the hot side of subcolling condenser 15 is cooled to -110 DEG C from low temperature
The liquid inlet for washing 11 top of tower enters in cold washing tower 11.
Cooling point of level Four of flue gas is cooling in the utility model: the first order is cooled down with circulating cooling water of power plant, water cooling
Temperature at 2 cold side input port of heat exchanger is 30 DEG C, and the temperature of 2 cold side outlet of water cooling heat exchanger is 40 DEG C；The second level is with cold
Water dispenser group 6 is cooling, and water cooler 6 uses screw water cooling machine set, and the leaving water temperature of water cooler 6 is -5 DEG C, Energy Efficiency Ratio COP=
5；The third level is cooled down by exchanging heat with low temperature neat stress, and heat exchange difference is 20 DEG C；The fourth stage is sprayed by low temperature normal propyl alcohol
Cooling, cooling capacity is provided by Cryo Refrigerator 16, and evaporating temperature is -115 DEG C, COP=0.8.
100,000 mark side of exhaust gas volumn in the present embodiment, inlet temperature are 50 DEG C, water content 11%, and gas concentration lwevel is
12%.4.5 ton/hours are drained after water cooled heat exchanger 2 is cooling, drains 2.75 ton/hours after low temperature dehumidification device 5 is cooling, point
Son sieve dehumidifier 8 is dehydrated 0.2 ton/hour.90% carbon dioxide is recycled through dry ice in flue gas, produces 18 ton/hours of dry ice, always
Power consumption is 5MW, and power consumption is 5000 kilowatt hours per hour, and dry ice energy consumption per ton is 278 kilowatt hours.
Through practicing, the utility model from flue gas in practical application, capture the dry ice conversion ratio of the carbon dioxide to get off
It is 100%, high conversion rate；And traditional flue gas decarbonization-compress and liquefy-dry ice technology path conversion ratio processed is less than 40%.In addition,
The production cost of dry ice per ton is lower than 200 yuan in the utility model, and traditional flue gas decarbonization-compresses and liquefies-dry ice technology processed
Route cost is higher than 600 yuan, and production cost reduces by 3 times.Meanwhile flue gas decarbonization energy consumption cost is lower, is lower than 100 yuan/ton of CO2,
Than traditional decarbonization system energy saving cost 40%-50%.
Claims (5)
1. a kind of device of off-gas recovery dry ice, which is characterized in that including air-introduced machine (1), power plant FGD exiting flue gas pipeline, water
Cold heat exchanger (2), the first gas-liquid separator (4), low temperature dehumidification device (5), the second gas-liquid separator (7), molecular sieve dehumidifier
(8), cold recovery exchanger (10), cold washing tower (11), smoke exhaust system, solid-liquid separator (13), subcolling condenser
(15), circulation (3) and water cooler (6)；
The entrance of air-introduced machine (1) is connected with power plant FGD exiting flue gas pipeline, the water cooled heat exchanger in outlet (2) of air-introduced machine (1)
Hot side be connected with the entrance of the first gas-liquid separator (4), the gas side of the first gas-liquid separator (4) is exported through low temperature dehumidification device
(5) hot side is connected with the entrance of the second gas-liquid separator (7), the gas side outlet of the second gas-liquid separator (7) and molecular sieve
The entrance of dehumidifier (8) is connected, and the outlet of molecular sieve dehumidifier (8) is washed through the hot side of cold recovery exchanger (10) with low temperature
The gas access for washing tower (11) bottom is connected, the exhanst gas outlet at the top of cold washing tower (11) and cold recovery exchanger (10)
Cold side input port be connected, the cold side outlet port of cold recovery exchanger (10) is connected with smoke exhaust system, cold washing tower
(11) entrance of the serum outlet with solid-liquid separator (13) of bottom is connected, the liquid outlet and low temperature of solid-liquid separator (13)
The hot side entrance of cooler (15) is connected, the hot side outlet of subcolling condenser (15) and the liquid of cold washing tower (11) upper end
Entrance is connected；
The cold side of water cooling heat exchanger (2) is connected with circulation (3), the cold side and water cooler (6) of low temperature dehumidification device (5)
It is connected, the cold side of subcolling condenser (15) is connected with Cryo Refrigerator (16).
2. the device of off-gas recovery dry ice according to claim 1, which is characterized in that further include header tank (9), the first gas
The discharge outlet of the discharge outlet of liquid/gas separator (4), the discharge outlet of the second gas-liquid separator (7) and molecular sieve dehumidifier (8) with catchment
The entrance of case (9) is connected.
3. the device of off-gas recovery dry ice according to claim 1, which is characterized in that the slurry of cold washing tower (11) bottom
Liquid outlet is connected through low temperature slurries pump (12) with solid-liquid separator (13) entrance.
4. the device of off-gas recovery dry ice according to claim 1, which is characterized in that the liquid discharge of solid-liquid separator (13)
Mouth surveys entrance with the heat of subcolling condenser (15) through low-temperature circulating pump (14) and is connected.
5. the device of off-gas recovery dry ice according to claim 1, which is characterized in that further include refrigerant replenishment system (18)
And dry ice molding machine (17), wherein the refrigerant inlet of solid-liquid separator (13) is connected with refrigerant replenishment system (18), solid-liquid point
Solid outlet from device (13) is connected with dry ice molding machine (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821697278.9U CN208990490U (en) | 2018-10-18 | 2018-10-18 | A kind of device of off-gas recovery dry ice |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821697278.9U CN208990490U (en) | 2018-10-18 | 2018-10-18 | A kind of device of off-gas recovery dry ice |
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| Publication Number | Publication Date |
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| CN208990490U true CN208990490U (en) | 2019-06-18 |
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| CN201821697278.9U Active CN208990490U (en) | 2018-10-18 | 2018-10-18 | A kind of device of off-gas recovery dry ice |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111595655A (en) * | 2020-06-16 | 2020-08-28 | 云南锡业股份有限公司锡业分公司 | Pretreatment device and pretreatment method for online analysis sample gas of tin smelting flue gas |
| WO2022032859A1 (en) * | 2020-08-14 | 2022-02-17 | 中国华能集团清洁能源技术研究院有限公司 | Low-temperature pentane-washing carbon dioxide capture system and method |
| CN111595655B (en) * | 2020-06-16 | 2024-04-30 | 云南锡业股份有限公司锡业分公司 | Pretreatment device and pretreatment method for on-line analysis of sample gas of tin smelting flue gas |
-
2018
- 2018-10-18 CN CN201821697278.9U patent/CN208990490U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111595655A (en) * | 2020-06-16 | 2020-08-28 | 云南锡业股份有限公司锡业分公司 | Pretreatment device and pretreatment method for online analysis sample gas of tin smelting flue gas |
| CN111595655B (en) * | 2020-06-16 | 2024-04-30 | 云南锡业股份有限公司锡业分公司 | Pretreatment device and pretreatment method for on-line analysis of sample gas of tin smelting flue gas |
| WO2022032859A1 (en) * | 2020-08-14 | 2022-02-17 | 中国华能集团清洁能源技术研究院有限公司 | Low-temperature pentane-washing carbon dioxide capture system and method |
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