CN204601956U - Produce the system of food-grade carbon-dioxide - Google Patents
Produce the system of food-grade carbon-dioxide Download PDFInfo
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- CN204601956U CN204601956U CN201520268371.8U CN201520268371U CN204601956U CN 204601956 U CN204601956 U CN 204601956U CN 201520268371 U CN201520268371 U CN 201520268371U CN 204601956 U CN204601956 U CN 204601956U
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- regenerator
- heat exchanger
- liquid heat
- dioxide
- pump
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Abstract
The utility model discloses a kind of system of producing food-grade carbon-dioxide, to solve current limekiln tail gas without recycling directly discharge, large and effective and reasonablely can not utilize the problem of resource to environmental hazard.This system comprises absorption tower, poor rich liquid heat exchanger, rich solution pump, poor rich liquid heat exchanger, regenerator, absorption tower is connected with rich solution pump, rich solution pump is connected with poor rich liquid heat exchanger, being connected with regenerator of poor rich liquid heat exchanger, the bottom of regenerator is provided with reboiler, the tower top of described regenerator is connected with regeneration gas condenser, and regeneration gas condenser is connected with gas-liquid separator.The utility model takes low pressure decarburization technique, significantly reduces the carbon emission of limekiln tail gas, and produces food-grade carbon-dioxide by purifying, and meets environmentally friendly and economic development requirement that is resource-conserving.Add reclaiming device, avoid the rotten of MEA solution.
Description
Technical field
the utility model belongs to chemical field, is specifically related to the system of producing food-grade carbon-dioxide.
Background technology
Carbon dioxide is a kind of industrial chemicals of having many uses; be widely used in various beverage, food IQF and preserve fresh-keeping, protection-gas welding, booth gas fertilizer, tobacco expanding agent, supercritical extract agent etc.; as chemical carbon source in a large number for the production of urea, carbonic ester, Merlon, aspirin and synthesizing methanol, be also main greenhouse gases.
Existing document discloses the method utilizing limekiln using waste heat from tail gas to carry out concrete segment production, but the device of carbon dioxide in its non-Appropriate application tail gas.
Utility model content
The purpose of this utility model is to provide the system of a kind of limekiln End gas production food-grade carbon-dioxide, to solve current limekiln tail gas without recycling directly discharge, large and effective and reasonablely can not utilize the problem of resource to environmental hazard.
The system of a kind of limekiln End gas production food-grade carbon-dioxide, comprise absorption tower, poor rich liquid heat exchanger, rich solution pump, poor rich liquid heat exchanger, regenerator, absorption tower is connected with rich solution pump, rich solution pump is connected with poor rich liquid heat exchanger, being connected with regenerator of poor rich liquid heat exchanger, the bottom of regenerator is provided with reboiler, and the tower top of described regenerator is connected with regeneration gas condenser, and regeneration gas condenser is connected with gas-liquid separator.
Preferably, described poor rich liquid heat exchanger is also connected with lean solution water cooler by lean pump, and the other end of lean solution water cooler is connected with absorption tower.
Preferably, lean pump is also connected with amine and reclaims heater, and amine reclaims heater connection and joins alkali groove.
The utility model takes low pressure decarburization technique concentrate and produces CO
2product.By exploitation limekiln tail gas recycle recycling project, be conducive to the further optimization of industrial chain, focus on ecological, environmental protective, cost-saving, improve competitiveness and the competitiveness of product in market of company.Feature is as follows:
1. contain great amount of carbon dioxide composition in the tail gas of limekiln, carbon dioxide is that a kind of pernicious gas freely discharges and can cause very large pollution to environment, but carbon dioxide is again that broad-spectrum industrial raw materials comprises that food processing is fresh-keeping simultaneously, beverage, chemical fertilizer, fire prevention, oil exploitation is all from not carbon dioxide.The utility model and ecological, environmental protective, again can cost-saving improve effects.
2., from the tail gas that lime kiln device is sent here, first after water ring vacuum pump extracts, send into CO
2absorption tower, CO in process
2bring a large amount of steam in air-flow into, can dilute MEA solution, we are again by CO
2de-watering apparatus is added before sending into absorption tower.
3. in order to strengthen CO
2the absorbability on absorption tower and effect, separately draw a decarburization rich solution pipeline and enter recycle liquid pump at the bottom of tower, and pressurization Posterior circle sends into CO
2enter in the middle part of absorption tower in tower and carry out cyclic absorption.
4. in the cyclic process of MEA solution, need to carry out rich or poor liquid conversion by the mode of heat exchange, the too fast meeting of MEA solution flow rate causes the CO of last release
2gas is very few, and we change the MEA solution flow rate of rich solution pump, make CO
2can discharge in a large number.
5. rich solution can bring steam into after Steam Heating, does not enter whole cyclic process, with CO to this part steam
2enter gas-liquid separator, directly discharge after cooling.
In 6.MEA decarbonizing process, owing to there being O
2to there is solution perishable, regeneration process need be carried out.We carry out regeneration process by drawing one MEA lean solution from lean pump shunting to amine recovery heater.
7. whole CO
2in absorption and regeneration process, because MEA solution goes bad, will a small amount of oxazolidone-2,1-(2-hydroxyethyl be generated)-imidazolone-2, N-(2-hydroxyethyl) impurity such as an ethylenediamine, we are provided with amine and reclaim heater and carry out regeneration and process.
The utility model advantage is as follows: 1. take low pressure decarburization technique, significantly reduces the carbon emission of limekiln tail gas, and produces food-grade carbon-dioxide by purifying, and meets environmentally friendly and economic development requirement that is resource-conserving.2. add reclaiming device, avoid the rotten of MEA solution.
Accompanying drawing explanation
Fig. 1 is the structural representation of the system of a kind of limekiln End gas production food-grade carbon-dioxide.
Reference numeral implication is as follows: water ring vacuum pump (P102), absorption tower (T102), regenerator (T103), rich solution pump (P106), regenerated liquid recovery pump (P110), lean pump (P107), lean solution water cooler (E102), poor rich liquid heat exchanger (E103), amine reclaims heater (E104), reboiler (E105), regeneration gas condenser (E106), join alkali groove (V101), gas-liquid separator (V110), cleaning solution storage tank (V104).
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described in more detail.
As shown in the figure, the system of a kind of limekiln End gas production food-grade carbon-dioxide, comprise absorption tower T102, poor rich liquid heat exchanger E103, rich solution pump P106, poor rich liquid heat exchanger E103, regenerator T103, absorption tower T102 is connected with rich solution pump P106, rich solution pump P106 is connected with poor rich liquid heat exchanger E103, poor rich liquid heat exchanger E103 is connected with regenerator T103, the bottom of regenerator T103 is provided with reboiler E105, the tower top of regenerator T103 is connected with regeneration gas condenser E106, and regeneration gas condenser E106 is connected with gas-liquid separator V110.Poor rich liquid heat exchanger E103 is also connected with lean solution water cooler E102 by lean pump P107, and the other end of lean solution water cooler E102 is connected with absorption tower T102.Lean pump P107 is also connected with amine and reclaims heater E104, and amine recovery heater E104 connects respectively and joins alkali groove V101 and regenerator T103.
Citing below utilizes this utility model system to prepare food-grade carbon-dioxide and recycles, regenerates the process of process.
Embodiment 1-prepares food-grade carbon-dioxide:
A, from the limekiln tail gas out-of-bounds come, tolerance 9000 Nm
3, mass percentage 22 %, pressure, 3 kPa, temperature 32 DEG C, enters after water ring vacuum pump P102 is forced into 50 kPa, by dehydration, sends into carbon dioxide absorption tower T02, the CO in tail gas
2be dissolved in ethanolamine solutions (MEA) solution by absorption;
Rich solution pump P106 introduced by B, the MEA rich solution managed from T102 tower bottom, absorption tower, send into poor rich liquid heat exchanger E103 after being forced into 0.6 MPa to be warming up to 95 DEG C and to enter carbon-dioxide regenerating tower T103 tower top, one reboiler E105 is set bottom regenerator T103 and utilizes Steam Heating, control bottom temperature at 120 DEG C, 0.15MPa, tower top temperature 95 DEG C, 0.12 Mpa; The flow velocity of rich solution pump P106 is 80m
3/ h.
C, regenerator T103 tower top arrange a regeneration gas condenser E106, regeneration gas are cooled to 50 DEG C, and after gas-liquid separator V110 is separated, liquid returns regenerator T103 through regenerated liquid recovery pump P110, the CO of separation
2gas sends battery limit (BL) as gas product, and compressed process obtains finished product.The CO be separated
2gas product obtains finished product 3.63t after compression, productive rate 93.3%.
Embodiment 2-recycles
The MEA circulation cleaning lean solution come from regenerator T103 in embodiment 1, temperature 120 DEG C, after poor rich liquid heat exchanger E103 heat exchange is cooled to 65 DEG C, enters lean pump P107 is pressurized to 0.45 MPa, from lean pump P107, shunting one lean solution other enters lean solution water cooler E102 and is cooled to 40 DEG C further, absorption tower T102 tower top is entered after mechanical filter, activated carbon filtration, recycle, with limekiln tail gas counter current contacting, the CO in tail gas
2dissolved.
Rich solution pump (P106) is connected with the decarburization rich solution pipeline at the bottom of absorption tower (T102) tower, and after pressurization, ethanolamine solutions lean solution circulation feeding absorption tower (T102) middle part enters in tower and carries out cyclic absorption.
Embodiment 3-regenerates process
Drawing one monoethanolamine lean solution through poor rich liquid heat exchanger (E103) liquid out through lean pump (P107) and reclaim heater (E104) to amine and carry out regeneration and process in embodiment 1, first enter from the solid base out-of-bounds come and join alkali groove (V101), together choline process is carried out with desalted water, enter amine after the alkali lye prepared mixes with desalted water and reclaim heater (E104), amine reclaims heater and utilizes Steam Heating, and temperature controls at 130 DEG C.The ethanolamine solutions of regeneration sends regenerator T103 back to, and the rotten monoethanolamine waste liquid of regeneration sends into boiler burning disposal.
Owing to will go bad in monoethanolamine decarbonizing process, regeneration process must be carried out.Fill into fresh ethanolamine solutions from cleaning solution storage tank (V104) interruption or continuous print and enter absorption tower (T102) circulation cleaning.
Embodiment 4-prepares food-grade carbon-dioxide:
A, limekiln tail gas, tolerance 15000Nm
3, content 25 %, pressure, 4 kPa, temperature 36 DEG C, enters after water ring vacuum pump P102 is forced into 52kPa, by dehydration, sends into carbon dioxide absorption tower T02, the CO in tail gas
2be dissolved in MEA solution by absorption;
Rich solution pump P106 introduced by B, the MEA rich solution managed from T102 tower bottom, absorption tower, send into poor rich liquid heat exchanger E103 after being forced into 0.62 MPa to be warming up to 100 DEG C and to enter carbon-dioxide regenerating tower T103 tower top, one reboiler E105 is set bottom regenerator T103 and utilizes Steam Heating, control bottom temperature at 125 DEG C, 0.17MPa, tower top temperature 100 DEG C, 0.14MPa.The flow velocity of rich solution pump (P106) is 85m
3/ h.
C, regenerator T103 tower top arrange a regeneration gas condenser E106, regeneration gas are cooled to 55 DEG C, and after gas-liquid separator V110 is separated, liquid returns regenerator T103 through regenerated liquid recovery pump P110, the CO of separation
2gas sends battery limit (BL) as gas product, and compressed process obtains finished product.The CO be separated
2gas product obtains finished product 7.14t after compression, productive rate 96.9%.
Embodiment 5-recycles
The MEA circulation cleaning lean solution come from regenerator T103 in embodiment 4, temperature 125 DEG C, after poor rich liquid heat exchanger E103 heat exchange is cooled to 70 DEG C, enters lean pump P107 is pressurized to 0.47 MPa, shunting one lean solution other enters lean solution water cooler E102 and is cooled to 42 DEG C further, absorption tower T102 tower top is entered after mechanical filter, activated carbon filtration, recycle, with limekiln tail gas counter current contacting, the CO in tail gas
2dissolved.
Rich solution pump (P106) is connected with the decarburization rich solution pipeline at the bottom of absorption tower (T102) tower, and after pressurization, ethanolamine solutions lean solution circulation feeding absorption tower (T102) middle part enters in tower and carries out cyclic absorption.
Embodiment 6-regenerates process
Drawing one monoethanolamine lean solution through poor rich liquid heat exchanger (E103) liquid out through lean pump (P107) and reclaim heater (E104) to amine and carry out regeneration and process in embodiment 4, first enter from the solid base out-of-bounds come and join alkali groove (V101), together choline process is carried out with desalted water, enter amine after the alkali lye prepared mixes with desalted water and reclaim heater (E104), amine reclaims heater and utilizes Steam Heating, and temperature controls at 135 DEG C.The ethanolamine solutions of regeneration sends regenerator T103 back to, and the rotten monoethanolamine waste liquid of regeneration sends into boiler burning disposal.
Owing to will go bad in monoethanolamine decarbonizing process, regeneration process must be carried out.Fill into fresh ethanolamine solutions from cleaning solution storage tank (V104) interruption or continuous print and enter absorption tower (T102) circulation cleaning.
Embodiment 7-prepares food-grade carbon-dioxide:
A, limekiln tail gas, tolerance 13000Nm
3, content 24 %, pressure, 5 kPa, temperature 40 DEG C, enters after water ring vacuum pump P102 is forced into 48kPa, by dehydration, sends into carbon dioxide absorption tower T02, the CO in tail gas
2be dissolved in MEA solution by absorption,
Rich solution pump P106 introduced by B, the MEA rich solution managed from T102 tower bottom, absorption tower, send into poor rich liquid heat exchanger E103 after being forced into 0.58 MPa to be warming up to 105 DEG C and to enter carbon-dioxide regenerating tower T103 tower top, one reboiler E105 is set bottom regenerator T103 and utilizes Steam Heating, control bottom temperature at 130 DEG C, 0.13MPa, tower top temperature 105 DEG C, 0.10MPa.The flow velocity of rich solution pump (P106) is 75m
3/ h.
C, regenerator T103 tower top arrange a regeneration gas condenser E106, regeneration gas are cooled to 60 DEG C, and after gas-liquid separator V110 is separated, liquid returns regenerator T103 tower top through regenerated liquid recovery pump P110, the CO of separation
2gas sends battery limit (BL) as gas product, and compressed process obtains finished product.The CO be separated
2gas product obtains finished product 5.88t after compression, productive rate 95.9%.
Embodiment 8-recycles
The MEA circulation cleaning lean solution come from regenerator T103 in embodiment 7, temperature 130 DEG C, after poor rich liquid heat exchanger E103 heat exchange is cooled to 75 DEG C, enters lean pump P107 is pressurized to 0.43MPa, one lean solution enters lean solution water cooler E102 and is cooled to 38 DEG C further in addition, absorption tower T102 tower top is entered after mechanical filter, activated carbon filtration, recycle, with limekiln tail gas counter current contacting, the CO in tail gas
2dissolved.
Rich solution pump (P106) is connected with the decarburization rich solution pipeline at the bottom of absorption tower (T102) tower, and after pressurization, ethanolamine solutions lean solution circulation feeding absorption tower (T102) middle part enters in tower and carries out cyclic absorption.
Embodiment 9-regenerates process
Drawing one monoethanolamine lean solution through poor rich liquid heat exchanger (E103) liquid out through lean pump (P107) and reclaim heater (E104) to amine and carry out regeneration and process in embodiment 7, first enter from the solid base out-of-bounds come and join alkali groove (V101), together choline process is carried out with desalted water, enter amine after the alkali lye prepared mixes with desalted water and reclaim heater (E104), amine reclaims heater and utilizes Steam Heating, and temperature controls at 125 DEG C.The ethanolamine solutions of regeneration sends regenerator T103 back to, and the rotten monoethanolamine waste liquid of regeneration sends into boiler burning disposal.
Owing to will go bad in monoethanolamine decarbonizing process, regeneration process must be carried out.Fill into fresh ethanolamine solutions from cleaning solution storage tank (V104) interruption or continuous print and enter absorption tower (T102) circulation cleaning.
Claims (3)
1. the system of a limekiln End gas production food-grade carbon-dioxide, comprise absorption tower (T102), poor rich liquid heat exchanger (E103), it is characterized in that: it also comprises rich solution pump (P106), poor rich liquid heat exchanger (E103), regenerator (T103), absorption tower (T102) is connected with rich solution pump (P106), rich solution pump (P106) is connected with poor rich liquid heat exchanger (E103), being connected with regenerator (T103) of poor rich liquid heat exchanger (E103), the bottom of regenerator (T103) is provided with reboiler (E105), the tower top of described regenerator (T103) is connected with regeneration gas condenser (E106), regeneration gas condenser (E106) is connected with gas-liquid separator (V110).
2. the system of limekiln according to claim 1 End gas production food-grade carbon-dioxide, it is characterized in that: described poor rich liquid heat exchanger (E103) is also connected with lean solution water cooler (E102) by lean pump (P107), and the other end of lean solution water cooler (E102) is connected with absorption tower (T102).
3. the system of limekiln according to claim 1 and 2 End gas production food-grade carbon-dioxide, it is characterized in that: lean pump (P107) is also connected with amine and reclaims heater (E104), amine recovery heater (E104) connects respectively joins alkali groove (V101) and regenerator (T103).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520268371.8U CN204601956U (en) | 2015-04-29 | 2015-04-29 | Produce the system of food-grade carbon-dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520268371.8U CN204601956U (en) | 2015-04-29 | 2015-04-29 | Produce the system of food-grade carbon-dioxide |
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|---|---|
| CN204601956U true CN204601956U (en) | 2015-09-02 |
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|---|---|---|---|
| CN201520268371.8U Expired - Fee Related CN204601956U (en) | 2015-04-29 | 2015-04-29 | Produce the system of food-grade carbon-dioxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104857816A (en) * | 2015-04-29 | 2015-08-26 | 古浪鑫辉化工有限公司 | System and method for producing food grade carbon dioxide through lime kiln tail gases |
| CN108144420A (en) * | 2018-01-23 | 2018-06-12 | 陕西科技大学 | A kind of supercritical water oxidation excess oxygen reclamation system |
| CN114405246A (en) * | 2021-12-28 | 2022-04-29 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
-
2015
- 2015-04-29 CN CN201520268371.8U patent/CN204601956U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104857816A (en) * | 2015-04-29 | 2015-08-26 | 古浪鑫辉化工有限公司 | System and method for producing food grade carbon dioxide through lime kiln tail gases |
| CN104857816B (en) * | 2015-04-29 | 2017-04-12 | 古浪鑫辉化工有限公司 | System and method for producing food grade carbon dioxide through lime kiln tail gases |
| CN108144420A (en) * | 2018-01-23 | 2018-06-12 | 陕西科技大学 | A kind of supercritical water oxidation excess oxygen reclamation system |
| CN108144420B (en) * | 2018-01-23 | 2023-06-16 | 陕西科技大学 | Supercritical water oxidation excess oxygen recovery system |
| CN114405246A (en) * | 2021-12-28 | 2022-04-29 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
| CN114405246B (en) * | 2021-12-28 | 2022-11-01 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
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|---|---|---|---|
| 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: 20150902 Termination date: 20160429 |