CN209668781U - The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal - Google Patents
The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal Download PDFInfo
- Publication number
- CN209668781U CN209668781U CN201920314153.1U CN201920314153U CN209668781U CN 209668781 U CN209668781 U CN 209668781U CN 201920314153 U CN201920314153 U CN 201920314153U CN 209668781 U CN209668781 U CN 209668781U
- Authority
- CN
- China
- Prior art keywords
- tower
- pipeline
- supplement
- carbon dioxide
- cooler
- 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.)
- Active
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 34
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 34
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 30
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 21
- 239000012535 impurity Substances 0.000 title claims abstract description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 80
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 40
- 239000013589 supplement Substances 0.000 claims abstract description 35
- 239000002808 molecular sieve Substances 0.000 claims abstract description 20
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 18
- 238000001035 drying Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 8
- 230000007062 hydrolysis Effects 0.000 claims abstract description 8
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 8
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 8
- 239000011593 sulfur Substances 0.000 claims abstract description 8
- 230000008676 import Effects 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 5
- 239000002274 desiccant Substances 0.000 claims description 3
- 238000007873 sieving Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 13
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 11
- 230000008569 process Effects 0.000 abstract description 11
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 51
- 239000007788 liquid Substances 0.000 description 16
- 239000007791 liquid phase Substances 0.000 description 11
- 238000006477 desulfuration reaction Methods 0.000 description 10
- 239000012071 phase Substances 0.000 description 10
- 230000023556 desulfurization Effects 0.000 description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000002440 industrial waste Substances 0.000 description 3
- 230000001502 supplementing effect Effects 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000020335 dealkylation Effects 0.000 description 2
- 238000006900 dealkylation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 125000000467 secondary amino group Chemical class [H]N([*:1])[*:2] 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The utility model relates to a kind of systems of lighter hydrocarbons impurity in novel carbon dioxide removal, including pretreatment system, desulphurization system, ammonia cooling system, heat exchanger, molecular sieve drying tower, purifying column；Pretreatment system includes passing through the sequentially connected booster fan of pipeline, Gas Cooler and compressor；Desulphurization system includes passing through the sequentially connected water cooler of pipeline, pre- desulfurizing tower, hydrolysis tower and fine de-sulfur tower；Ammonia cooling system includes level-one ammonia cooler and second level ammonia cooler；It further include supplement knockout tower, the lower part supplemented in knockout tower is provided with the first coil pipe；The utility model replaces the de- hydrocarbon process in traditional handicraft by supplement knockout tower, effectively reduces input cost and operation expense；The utility model has the advantages that effectively improve that carbon dioxide purity, process are simple, overall cost is low, save the energy.
Description
Technical field
The utility model belongs to titanium dioxide tower purification technique field, and in particular to lighter hydrocarbons in a kind of novel carbon dioxide removal
The system of impurity.
Background technique
Rich carbonated industrial waste gas can be discharged in production of synthetic ammonia, and carbon dioxide is to lead to greenhouse effects
The gas of generation, therefore in order to avoid the deterioration of atmospheric environment, match again after needing to extract the industrial waste gas carbon dioxide
Side is into atmosphere.
The process flow for the industrial waste gas that processing production of synthetic ammonia generates at present are as follows: unstripped gas ----cooling ----pressure
Contracting ----desulfurization --- de- hydrocarbon --- dry --- purification --- finished product.Wherein, when carrying out de- hydrocarbon process to unstripped gas, capital equipment
It is dealkylation tower, has two auxiliary heat-exchanging equipment, oxygen supply (or oxygen-enriched) equipment in dealkylation tower rear and front end, an electric heating is set
Standby and indicating meter, connecting pipeline etc., it is relatively more to be related to equipment, and connection process is complex；Moreover, de- hydrocarbon is former
Reason is that the combustible component and oxygen in impurity react generation carbon dioxide eliminating, because the combustible components amount such as methane is few, under normal circumstances
It cannot react with oxygen, it is necessary to could occur under special-purpose catalyst and high temperature, catalyst value is high, and has using week
Phase needs timing to replace, heating when driving and also high for power consumption needed for maintaining reaction temperature, so as to cause the comprehensive of de- hydrocarbon ring section
Close higher cost.
On the other hand, due to the change of unstripped gas supply unit steps, the unstripped gas impurity component of supply is caused to become
Change, total hydrocarbon content rises to 1500ppm from 800ppm, and methane ratio accounts for 90%.Make the de- hydrocarbon scarce capacity of device, finally
Cause product purity to decline, be reduced to 98.9% by original 99.92, lower than the standard requirements of country 99.9%.To improve quality,
De- hydrocarbon load is increased, de- hydrocarbon temperature is increased to 450 DEG C or more, opens electric heating facility, increases energy consumption, finally not only significantly
Increase cost, and influence catalyst service life, operation difficulty increases, and safety is also affected.
Utility model content
A kind of raising carbon dioxide purity, process letter are provided the purpose of the utility model is to overcome the deficiencies in the prior art
The system that list, overall cost are low, save lighter hydrocarbons impurity in the novel carbon dioxide removal of the energy.
The technical solution of the utility model is under:
The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal, including pretreatment system, desulphurization system, ammonia cooling system
System, heat exchanger, molecular sieve drying tower, purifying column；
The pretreatment system includes passing through the sequentially connected booster fan of pipeline, Gas Cooler and compressor；
The desulphurization system includes passing through the sequentially connected water cooler of pipeline, pre- desulfurizing tower, hydrolysis tower and fine de-sulfur
Tower；
The heat source import of the heat exchanger is connected by pipeline with the outlet of compressor, and the thermal source outlet of heat exchanger is logical
Piping is connected with the import of water cooler, and the cold source import of heat exchanger passes through the outlet phase of pipeline and molecular sieve drying tower
Even；
The import of the molecular sieve drying tower is connected by pipeline with the outlet of fine de-sulfur tower；
The ammonia cooling system includes level-one ammonia cooler and second level ammonia cooler；
It further include supplement knockout tower, the top of the supplement knockout tower is connected by pipeline with the top of purifying column, is supplemented
The lower part of knockout tower is connected by pipeline with the lower part of purifying column, and the lower part for supplementing knockout tower also passes through pipeline and secondary amine is cooling
Device is connected；
Lower part in the supplement knockout tower is provided with the first coil pipe, and the import of first coil pipe is handed over by pipeline and heat
The cold source outlet of parallel operation is connected, and the outlet of the first coil pipe is connected by pipeline with level-one ammonia cooler, the level-one ammonia cooler
Outlet the middle part of purifying column is connected to by pipeline.
Further, the pipe joint being connected on the purifying column with molecular sieve drying tower is separated lower than on purifying column with supplement
The connected pipe joint of tower.
Further, the pipe joint being connected on the supplement knockout tower with purifying column is higher than on supplement knockout tower and secondary amine
The connected pipe joint of cooler.
Further, the desiccant in the molecular sieve drying tower is molecular sieve.
Further, first coil pipe is along the lower inner wall of supplement knockout tower at snakelike coiling.
Further, the outlet of the second level ammonia cooler is connected with storage tank by pipeline.
Compared with prior art, the utility model has the beneficial effects that
1, the utility model increases the sky of gas-liquid separation by adding supplement knockout tower in the system of removing lighter hydrocarbons impurity
Between and simple rectifying realize effective removing of on-condensible gas, abandoning hydro carbons magazine in carbon dioxide can only be by the biography of burning removal
System method exempts in the prior art the individually link of de- hydrocarbon, effectively solves the problems, such as that one methane of lighter hydrocarbons volatilizees from liquid phase, effectively
Improve the purity of liquid carbon dioxide；
2, the utility model is used to the waste heat in system by supplementing knockout tower, utilizes based on carbon dioxide
The heat of mixed gas realizes liquid to the liquid carbon dioxide of purified tower preliminary purification in supplement knockout tower as heat source
(a such as easy rectifier) is mutually boiled again, the on-condensible gas in liquid carbon dioxide is overflowed again, thus to industry situation dioxy
Change carbon effectively to be purified；
3, the utility model replaces the de-hydrocarbon system in traditional system, without setting by the setting of supplement knockout tower
De- hydrocarbon section is set, the removing of the lighter hydrocarbons magazine in carbon dioxide is realized at high temperature without special-purpose catalyst, is effectively reduced de-
The cost of lighter hydrocarbons magazine in removing carbon dioxide；
In short, the utility model effectively improves, carbon dioxide purification degree, process are simple, overall cost is low, save energy
The advantages of source.
Detailed description of the invention
Fig. 1 is the process flow chart of the utility model.
Wherein, 1, booster fan, 2, Gas Cooler, 3, compressor, 4, heat exchanger, 5, water cooler, 6, pre- desulfurizing tower,
7, hydrolysis tower, 8, fine de-sulfur tower, 9, molecular sieve drying tower, 10, supplement knockout tower, 11, purifying column, 12, level-one ammonia cooler,
13, second level ammonia cooler, the 14, first coil pipe, 15, storage tank.
Specific embodiment
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are without making creative work
Every other embodiment obtained, fall within the protection scope of the utility model.
According to Fig. 1, in a kind of novel carbon dioxide removal lighter hydrocarbons impurity system, including to out-of-bounds synthesis ammonia system
The unstripped gas to come is conveyed to carry out pretreated pretreatment system, carry out desulfurization operations to by pretreated unstrpped gas
Desulphurization system carries out cooling ammonia cooling system to processed unstrpped gas and liquid carbon dioxide respectively, realizes cold and hot friendship
The heat exchanger 4 changed, the molecular sieve drying tower 9 for being dehydrated to the unstrpped gas Jing Guo desulfurization process, for pair
The purifying column 11 that liquid carbon dioxide is purified；
The pretreatment system includes passing through the sequentially connected booster fan 1 of pipeline, Gas Cooler 2 and compressor 3,
The air inlet of middle booster fan 1 inputs unstrpped gas by pipeline, and roots blower can be used in booster fan 1；
The desulphurization system includes de- by the sequentially connected water cooler 5 of pipeline, pre- desulfurizing tower 6, hydrolysis tower 7 and essence
Sulphur tower 8 carries out triple desulfurization operations by pre- desulfurizing tower 6, hydrolysis tower 7 and fine de-sulfur tower 8 to after unstrpped gas progress water cooling,
To which the sulfur dioxide in unstrpped gas effectively be removed；
The heat source import of the heat exchanger 4 is connected by pipeline with the outlet of compressor 3, and the heat source of heat exchanger 4 goes out
Mouth is connected by pipeline with the import of water cooler 5, and the cold source import of heat exchanger 4 passes through pipeline and molecular sieve drying tower 9
Outlet is connected；
The import of the molecular sieve drying tower 9 is connected by pipeline with the outlet of fine de-sulfur tower 8, thus to de- by second level
The unstrpped gas of sulphur is effectively dehydrated；
The ammonia cooling system includes level-one ammonia cooler 12 and second level ammonia cooler 13；
It further include supplement knockout tower 10, the top of the supplement knockout tower 10 passes through the top phase of pipeline and purifying column 11
Even, the lower part of supplement knockout tower 10 is connected by pipeline with the lower part of purifying column 11, and the lower part of supplement knockout tower 10 also passes through pipe
Road is connected with second level ammonia cooler 13；
Lower part in the supplement knockout tower 10 is provided with the first coil pipe 14, and the import of first coil pipe 14 passes through pipeline
It is connected with the outlet of the cold source of heat exchanger 4, the outlet of the first coil pipe 14 is connected by pipeline with level-one ammonia cooler 12, and described one
The outlet of grade ammonia cooler 12 is connected to the middle part of purifying column 11 by pipeline.
In this implementation, led on the pipeline that the heat exchanger 4 is linked with the first coil pipe 14 and 11 lower part phase of purifying column
Bye-pass even, 11 bottom of purifying column are provided with the second coil pipe being connected with bye-pass, and the other end of second coil pipe passes through
Pipeline is connected with level-one ammonia cooler 12, wherein the setting form of the second coil pipe and identical as the setting form of the first coil pipe 14.
In the present embodiment, the pipe joint being connected on the purifying column 11 with molecular sieve drying tower 9 is lower than on purifying column 11
The pipe joint being connected with supplement knockout tower 10.
In the present embodiment, the pipe joint being connected on the supplement knockout tower 10 with purifying column 11 is higher than supplement knockout tower 10
The upper pipe joint being connected with second level ammonia cooler 13.
In this implementation, the desiccant in the molecular sieve drying tower 9 is molecular sieve.
In this implementation, first coil pipe 14 is along the lower inner wall of supplement knockout tower 10 at snakelike coiling.
In the present embodiment, the outlet of the second level ammonia cooler 13 is connected with storage tank 15 by pipeline.
Lighter hydrocarbons impurity process is as follows in the utility model carbon dioxide removal:
Pretreatment stage, the unstrpped gas being discharged from out-of-bounds synthesis ammonia system enter air cooling after the pressurization of booster fan 1
But device 2 is cooled down, and unstrpped gas after cooling enters compressor and forms pressure after three stage compression in 2.3-2.6Mpa, temperature
Spend the unstrpped gas at 95 DEG C -110 DEG C；
Desulfurization section, the unstrpped gas after pretreatment with certain pressure and high temperature enter the heat source of heat exchanger 4 into
Mouthful, unstrpped gas enters the entrance of water cooler 5 by the pipeline of the thermal source outlet of heat exchanger 4, cooling by water cooler 4
Unstrpped gas is successively by the preliminary desulfurization of pre- desulfurizing tower 6, the hydrolysis desulfurization, the desulfurization again of fine de-sulfur tower 8 of hydrolysis tower 7 afterwards
Afterwards, heat is entered by pipeline in 10 DEG C -20 DEG C of unstrpped gas using formation temperature after the dehydration and drying of molecular sieve drying tower 9
The cold source import of exchanger 4 passes through in heat exchanger 4 through the unstrpped gas by desulfurization section desulfurization process that cold source import enters
The unstrpped gas crossed and form 45 DEG C -55 DEG C after the heat exchange of the unstrpped gas of heat source import entrance, due to cold in heat exchanger 4
The effect of heat exchange, the unstrpped gas temperature of 4 thermal source outlet of heat exchanger is also at 45 DEG C -55 DEG C；
Lighter hydrocarbons remove section, and interior 45 DEG C -55 DEG C unstrpped gas a part after heat exchange of heat exchanger 4 is handed over through overheat
The pipeline of 4 cold source of parallel operation outlet enters the first coil pipe 14 in supplement knockout tower 10, and then unstrpped gas passes through the first coil pipe 14
Outlet enter level-one ammonia cooler 12, the branch pipe on pipeline that another part unstrpped gas is exported through 4 cold source of over-heat-exchanger
Road enters the second coil pipe in purifying column 11, and then it is cold by the outlet of the second coil pipe 14 to enter level-one ammonia for the part material gas
But device 12 form the gas-liquid mixture based on liquid carbon dioxide, gas through the unstrpped gas after cooling of level-one ammonia cooler 12
Liquid mixture enters purifying column 11 from middle part, and gas-liquid two-phase carries out interphase heat transfer mass transfer by counter current contacting in purifying column 11,
On-condensible gas in liquid phase enters gas phase, and the liquid in gas phase is transferred to liquid phase, and gas phase is pushed up in purifying column 11 and cooled down again by refrigerant,
Wherein the carbon dioxide in gas phase is condensed into the bottom that liquid phase runs down into purifying column 11 again, also, 11 bottom of purifying column
Second coil pipe realizes that liquid phase is boiled and discharge part on-condensible gas again to liquid phase, at this point, 11 top of purifying column is on-condensible gas mostly,
11 bottom of purifying column obtains almost pure liquid CO 2；
In order to sufficiently remove the on-condensible gas in liquid carbon dioxide, the liquid phase of 11 bottom of purifying column enters benefit by pipeline
The lower part of knockout tower 10 is filled, the liquid phase supplemented in knockout tower 10 floods the first coil pipe 14 completely, supplements the liquid in knockout tower 10
Mutually realize that liquid phase is boiled again under the Source of the first coil pipe 14, the rectifier of such as one supplement, so that not coagulating in liquid phase
Gas is escaped from liquid phase again, and the on-condensible gas of evolution enters 11 top of purifying column from the top of supplement knockout tower 10, is entered
Successively by refrigerant, carbon dioxide heel row is recycled in cooling to the on-condensible gas and 11 inner top gas phase of purifying column at 11 top of purifying column again
In the air, the high purity liquid carbon dioxide for supplementing 10 bottom of knockout tower is transported to storage after second level ammonia cooler 13 is further cooling
It is stored in tank.
Although the utility model is described in detail with reference to the foregoing embodiments, come for those skilled in the art
Say, it is still possible to modify the technical solutions described in the foregoing embodiments, or to part of technical characteristic into
Row equivalent replacement, within the spirit and principle of the utility model, any modification, equivalent replacement, improvement and so on should all
It is included within the scope of protection of this utility model.
Claims (6)
1. the system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal, including pretreatment system, desulphurization system, ammonia cooling system
System, heat exchanger (4), molecular sieve drying tower (9), purifying column (11), it is characterised in that:
The pretreatment system includes passing through the sequentially connected booster fan of pipeline (1), Gas Cooler (2) and compressor (3)；
The desulphurization system includes passing through the sequentially connected water cooler of pipeline (5), pre- desulfurizing tower (6), hydrolysis tower (7) and essence
Desulfurizing tower (8)；
The heat source import of the heat exchanger (4) is connected by pipeline with the outlet of compressor (3), the heat source of heat exchanger (4)
Outlet is connected by pipeline with the import of water cooler (5), and the cold source import of heat exchanger (4) is dry by pipeline and molecular sieve
The outlet of tower (9) is connected；
The import of the molecular sieve drying tower (9) is connected by pipeline with the outlet of fine de-sulfur tower (8)；
The ammonia cooling system includes level-one ammonia cooler (12) and second level ammonia cooler (13)；
It further include supplement knockout tower (10), the top of supplement knockout tower (10) passes through the top phase of pipeline and purifying column (11)
Even, the lower part of supplement knockout tower (10) is connected by pipeline with the lower part of purifying column (11), supplements the lower part of knockout tower (10) also
It is connected by pipeline with second level ammonia cooler (13)；
Lower part in supplement knockout tower (10) is provided with the first coil pipe (14), and the import of first coil pipe (14) passes through pipe
Road is connected with the outlet of the cold source of heat exchanger (4), and the outlet of the first coil pipe (14) passes through pipeline and level-one ammonia cooler (12) phase
Even, the outlet of the level-one ammonia cooler (12) is connected to the middle part of purifying column (11) by pipeline.
2. the system of lighter hydrocarbons impurity in novel carbon dioxide removal according to claim 1, it is characterised in that: the purification
The pipe joint being connected on tower (11) with molecular sieve drying tower (9) with supplement knockout tower (10) lower than being connected on purifying column (11)
Pipe joint.
3. the system of lighter hydrocarbons impurity in novel carbon dioxide removal according to claim 1, it is characterised in that: the supplement
The pipe joint being connected on knockout tower (10) with purifying column (11) is higher than in supplement knockout tower (10) and second level ammonia cooler (13)
Connected pipe joint.
4. the system of lighter hydrocarbons impurity in novel carbon dioxide removal according to claim 1, it is characterised in that: the molecule
Sieving the desiccant in drying tower (9) is molecular sieve.
5. the system of lighter hydrocarbons impurity in novel carbon dioxide removal according to claim 1, it is characterised in that: described first
Coil pipe (14) is along the lower inner wall of supplement knockout tower (10) at snakelike coiling.
6. the system of lighter hydrocarbons impurity in novel carbon dioxide removal according to claim 1-5, it is characterised in that:
The outlet of the second level ammonia cooler (13) is connected with storage tank (15) by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920314153.1U CN209668781U (en) | 2019-03-12 | 2019-03-12 | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920314153.1U CN209668781U (en) | 2019-03-12 | 2019-03-12 | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209668781U true CN209668781U (en) | 2019-11-22 |
Family
ID=68571437
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920314153.1U Active CN209668781U (en) | 2019-03-12 | 2019-03-12 | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209668781U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109704341A (en) * | 2019-03-12 | 2019-05-03 | 陕西裕隆气体有限公司 | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal |
-
2019
- 2019-03-12 CN CN201920314153.1U patent/CN209668781U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109704341A (en) * | 2019-03-12 | 2019-05-03 | 陕西裕隆气体有限公司 | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101874967B (en) | Process for removing acid gas with low-temperature methanol solution | |
| CN100404988C (en) | Air-containing coal bed gas liquefaction separation process and equipment | |
| CN104208978B (en) | A kind of Apparatus and method for of gas purification | |
| CN108106326B (en) | Method and device for recycling nitrogen in krypton-xenon refining process | |
| CN209668781U (en) | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal | |
| CN104986734A (en) | Synthesis ammonia and synthesis gas self-circulation cryogenic separation purifying device and purifying method thereof | |
| CN214371298U (en) | Carbon dioxide gathering liquefaction recovery device | |
| CN109704341A (en) | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal | |
| CN1952569A (en) | Process and equipment for liquefying air-containing coal-bed gas | |
| CN114459204A (en) | System and method for low-temperature capture, purification, liquefaction and separation of carbon dioxide tail gas in coal chemical industry | |
| CN104190200B (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN104692325A (en) | System for comprehensively recovering hydrogen and light hydrocarbons through single absorption and double desorption | |
| CN206073565U (en) | A kind of energy-saving device for preparing high purity liquid carbon dioxide | |
| CN114518016A (en) | Carbon dioxide capturing, liquefying and recycling device and method | |
| CN101054167A (en) | Technique for extracting high-purity hydrogen sulfide | |
| CN106440661A (en) | Energy-saving type device for preparing high-purity liquid carbon dioxide and method | |
| CN103666585B (en) | Coupling method and system for low-temperature methanol washing technology and CO2 compressing technology | |
| CN112361715B (en) | Cryogenic ethylene recovery process | |
| CN201359420Y (en) | Low temperature separation equipment of mine gas | |
| CN212842469U (en) | Single-tower cryogenic rectification argon recovery system with argon circulation and hydrogen circulation | |
| CN101493277B (en) | Low temperature separation method and apparatus for mine gas | |
| CN210048683U (en) | System for retrieve ethane in follow gas mixture | |
| CN203971683U (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN200979332Y (en) | Air-containing coal layer gas-liquid separation apparatus | |
| CN219829182U (en) | System for purifying phosphorus pentafluoride gas through liquid nitrogen cryogenic condensation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A novel system for removing light hydrocarbon impurities from carbon dioxide Granted publication date: 20191122 Pledgee: Bank of China Limited Lanzhou Xigu center sub branch Pledgor: SHAANXI YULONG GAS Co.,Ltd. Registration number: Y2024620000007 |