CN204125172U - Nitrogen cycle technique produces the system of CO - Google Patents
Nitrogen cycle technique produces the system of CO Download PDFInfo
- Publication number
- CN204125172U CN204125172U CN201420609821.0U CN201420609821U CN204125172U CN 204125172 U CN204125172 U CN 204125172U CN 201420609821 U CN201420609821 U CN 201420609821U CN 204125172 U CN204125172 U CN 204125172U
- Authority
- CN
- China
- Prior art keywords
- interchanger
- valve
- communicated
- throttling valve
- flash tank
- 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.)
- Withdrawn - After Issue
Links
Abstract
The utility model discloses a kind of system adopting nitrogen cycle technique to produce CO.Its system comprises dehydrogenation tower, denitrification column, demethanizing tower, interchanger, flash tank, pressure swing adsorber, interchanger, pressure charging valve, decompressor, throttling valve.The utility model is applicable to produce CO gas.Various equipment is connected successively with pipeline.Replace CO circulation with nitrogen cycle, system energy consumption can reduce by more than 5%, and its manufacture difficulty is low, and safer; Nitrogen cycle compressor and decompressor cost are far below CO circulator and decompressor cost, and operation and maintenance cost is lower.
Description
Technical field
The utility model relates to a kind of system and method producing CO, particularly for the system adopting nitrogen cycle technique to produce CO.
Background technology
The traditional process figure that current domestic usual ethylene glycol cryogenic separation device all adopts is shown in accompanying drawing 2, traditional process is: the synthetic gas of purification converges with the supercharging resolution gas come by PSA and compressed flashed vapour, enter ice chest, after E1, E2 cooling, enter the flash distillation of V01 flash tank, enter PSA after gas rewarming and carry hydrogen, propose the compression of hydrogen residue resolution gas and be incorporated to synthetic gas and enter ice chest; Liquid section flows to into the dehydrogenation of T02 tower, dehydrogenation tower flashed vapour rewarming out, and compression is incorporated to synthetic gas and enters ice chest formation circulation; Liquid section flows to into the denitrogenation of T04 denitrification column, obtains rich nitrogen at its top, and the methane-rich liquid come with demethanizing tower converges, and rewarming removes user's pipe network as burning gas; Rich CO liquid throttling bottom T04, enters T03 demethanizing tower, after removing methane, converges with the CO gas of expand rear CO gas and decompression evaporation, rewarming, recompression, after compression, except extracting part CO as product, all the other enter ice chest, respectively as thermal source and the low-temperature receiver of each vaporizer and condenser.For making up the re-heat deficiency loss of system, CO expander need be adopted to freeze, also having and adopting external complement liquid nitrogen to make up the loss of re-heat deficiency.
Summary of the invention
The purpose of this utility model overcomes the deficiencies in the prior art, provides a kind of nitrogen cycle technique to produce the system of CO.
A kind of system adopting nitrogen cycle technique to produce CO comprises dehydrogenation tower, denitrification column, demethanizing tower, First Heat Exchanger, second interchanger, first flash tank, second flash tank, pressure swing adsorber, 3rd interchanger, 4th interchanger, 5th interchanger, 6th interchanger, first pressure charging valve, second pressure charging valve, 3rd pressure charging valve, decompressor, first throttle valve, second throttle, 3rd throttling valve, 4th throttling valve, 5th throttling valve, 6th throttling valve, 7th throttling valve, 8th throttling valve, dehydrogenation tower first exports and is connected with pipeline with denitrification column through the 3rd throttling valve, and denitrification column first exports successively through the 3rd interchanger, 7th throttling valve is connected with pipeline with demethanizing tower, and demethanizing tower first exports through the 4th interchanger and the second flash tank with pipeline communication, and demethanizing tower is communicated with by piping loop with the 6th interchanger, and denitrification column is through the 8th throttling valve, 5th throttling valve is communicated with the second flash tank, and First Heat Exchanger is communicated with the second flash tank by the 5th throttling valve, and dehydrogenation tower is successively through First Heat Exchanger, second interchanger, first pressure charging valve, second interchanger, First Heat Exchanger, first flash tank, first throttle valve and dehydrogenation tower are with pipeline communication, and dehydrogenation tower is communicated with by piping loop with First Heat Exchanger, and the first flash tank is successively through First Heat Exchanger, second interchanger, pressure swing adsorber, second pressure charging valve, second interchanger, First Heat Exchanger, first flash tank is communicated with piping loop, and the first flash tank is successively through second throttle, First Heat Exchanger is communicated with dehydrogenation tower with pipeline, First Heat Exchanger and the second interchanger are with pipeline communication, second interchanger circulates with the 3rd pressure charging valve and is communicated with, denitrification column is communicated with by piping loop with the 5th interchanger, denitrification column and the 3rd interchanger with pipeline communication, the second interchanger successively with decompressor, 5th interchanger, 4th throttling valve, 3rd interchanger, second interchanger with pipeline formed circulation be communicated with, the second interchanger successively with decompressor, 6th interchanger, 4th interchanger, second interchanger is formed circulation with pipeline and is communicated with.
The advantage of present method: deep cooling region, because N and CO temperature of saturation is very close, therefore the degree of depth is separated and preferably reduces working pressure, to realize saving energy and reduce the cost.Therefore N, CO knockout tower working pressure all reduces, like this, for meeting the demand of products C O pressure by traditional process, must to the CO product pressurization of separating, simultaneously due to the demand of technique unit condensation evaporation each in ice chest, and make up the requirement of re-heat loss, just all adopt CO circulation technology; H2 and the CO separation requirement products C O pressure 5.5bar of typical synthetic gas preparing ethylene glycol, nitrogenous no requirement (NR) or roughing out.Therefore, this kind of technique just can adopt nitrogen circulation to replace CO circulation, realizes the separating effect of its processing requirement; Do not need step-down to be separated recompression owing to producing products C O, therefore, system energy consumption can reduce by more than 5%; Adopt nitrogen cycle compression process to replace CO loop compression technique, no matter recycle compressor or decompressor, its manufacture difficulty is low, and safer; Nitrogen cycle compressor and decompressor cost are far below CO circulator and decompressor cost, and operation and maintenance cost is lower.
Accompanying drawing explanation
Fig. 1 is that nitrogen cycle technique produces CO system flowchart;
Fig. 2 is that traditional C O circulation technology produces CO system flowchart;
In figure, dehydrogenation tower 1, denitrification column 2, demethanizing tower 3, First Heat Exchanger 4, second interchanger 5, first flash tank 6, second flash tank 7, pressure swing adsorber 8, the 3rd interchanger 9, the 4th interchanger 10, the 5th interchanger 11, the 6th interchanger 12, first pressure charging valve 13, second pressure charging valve 14, the 3rd pressure charging valve 15, decompressor 16, first throttle valve 17, second throttle 18, the 3rd throttling valve 19, the 4th throttling valve 20, the 5th throttling valve 21, the 6th throttling valve 22, the 7th throttling valve 23, the 8th throttling valve 24.
Embodiment
As shown in Figure 1, a kind of system adopting nitrogen cycle technique to produce CO comprises dehydrogenation tower 1, denitrification column 2, demethanizing tower 3, First Heat Exchanger 4, second interchanger 5, first flash tank 6, second flash tank 7, pressure swing adsorber 8, 3rd interchanger 9, 4th interchanger 10, 5th interchanger 11, 6th interchanger 12, first pressure charging valve 13, second pressure charging valve 14, 3rd pressure charging valve 15, decompressor 16, first throttle valve 17, second throttle 18, 3rd throttling valve 19, 4th throttling valve 20, 5th throttling valve 21, 6th throttling valve 22, 7th throttling valve 23, 8th throttling valve 24, dehydrogenation tower 1 first outlet is connected with pipeline with denitrification column 2 through the 3rd throttling valve 19, and denitrification column 2 first exports successively through the 3rd interchanger 9, 7th throttling valve 23 is connected with pipeline with demethanizing tower 3, and demethanizing tower 3 first exports through the 4th interchanger 10 and the second flash tank 7 with pipeline communication, and demethanizing tower 3 is communicated with by piping loop with the 6th interchanger 12, and denitrification column 2 is through the 8th throttling valve 24, 5th throttling valve 21 is communicated with the second flash tank 7, and First Heat Exchanger 4 is communicated with the second flash tank 7 by the 5th throttling valve 21, and dehydrogenation tower 1 is successively through First Heat Exchanger 4, second interchanger 5, first pressure charging valve 17, second interchanger 5, First Heat Exchanger 4, first flash tank 6, first throttle valve 17 and dehydrogenation tower 1 are with pipeline communication, and dehydrogenation tower 1 is communicated with by piping loop with First Heat Exchanger 4, and the first flash tank 6 is successively through First Heat Exchanger 4, second interchanger 5, pressure swing adsorber 8, second pressure charging valve 18, second interchanger 5, First Heat Exchanger 4, first flash tank 6 is communicated with piping loop, and the first flash tank 6 is successively through second throttle 18, First Heat Exchanger 4 is communicated with dehydrogenation tower 1 with pipeline, First Heat Exchanger 4 and the second interchanger 5 are with pipeline communication, second interchanger 5 circulates with the 3rd pressure charging valve 15 and is communicated with, denitrification column 2 is communicated with by piping loop with the 5th interchanger 11, denitrification column 2 and the 3rd interchanger 9 with pipeline communication, the second interchanger 5 successively with decompressor 16, 5th interchanger 11, 4th throttling valve 20, 3rd interchanger 9, second interchanger 5 with pipeline formed circulation be communicated with, the second interchanger 5 successively with decompressor 16, 6th interchanger 12, 4th interchanger 10, second interchanger 5 is formed circulation with pipeline and is communicated with.
As shown in Figure 1, the method that the nitrogen cycle technique of described system produces CO is: the synthetic gas of purification and the resolution gas of supercharging and converged by the supercharging resolution gas of pressure swing adsorber 8, after the cooling of First Heat Exchanger 4, second interchanger 5, enter the first flash tank 6 flash distillation; Enter pressure swing adsorber 8 after gas rewarming and carry hydrogen, propose the compression of hydrogen residue resolution gas and be incorporated to synthetic gas and enter First Heat Exchanger 4 and cool, liquid enters dehydrogenation tower 1 dehydrogenation through first throttle valve 17; Dehydrogenation tower 2 flashed vapour out enters denitrification column 2 denitrogenation gas, obtains rich nitrogen at its top, and converge with demethanizing tower 3 methane-rich liquid out, rewarming removes user's pipe network as burning gas; Bottom liquid enters demethanizing tower 3 demethanizing, after removing methane, obtains CO product, is the re-heat deficiency loss making up system, adopts nitrogen circulation to be respectively used to the thermal source of each vaporizer and condenser and low-temperature receiver and nitrogen expansion machine swell refrigeration.
Claims (1)
1. the system adopting nitrogen cycle technique to produce CO, it is characterized in that comprising dehydrogenation tower (1), denitrification column (2), demethanizing tower (3), First Heat Exchanger (4), second interchanger (5), first flash tank (6), second flash tank (7), pressure swing adsorber (8), 3rd interchanger (9), 4th interchanger (10), 5th interchanger (11), 6th interchanger (12), first pressure charging valve (13), second pressure charging valve (14), 3rd pressure charging valve (15), decompressor (16), first throttle valve (17), second throttle (18), 3rd throttling valve (19), 4th throttling valve (20), 5th throttling valve (21), 6th throttling valve (22), 7th throttling valve (23), 8th throttling valve (24), dehydrogenation tower (1) first outlet is connected with pipeline with denitrification column (2) through the 3rd throttling valve (19), and denitrification column (2) first exports successively through the 3rd interchanger (9), 7th throttling valve (23) is connected with pipeline with demethanizing tower (3), demethanizing tower (3) first exports through the 4th interchanger (10) and the second flash tank (7) with pipeline communication, demethanizing tower (3) is communicated with by piping loop with the 6th interchanger (12), and denitrification column (2) is through the 8th throttling valve (24), 5th throttling valve (21) is communicated with the second flash tank (7), and First Heat Exchanger (4) is communicated with the second flash tank (7) by the 5th throttling valve (21), and dehydrogenation tower (1) is successively through First Heat Exchanger (4), second interchanger (5), first pressure charging valve (17), second interchanger (5), First Heat Exchanger (4), first flash tank (6), first throttle valve (17) and dehydrogenation tower (1) are with pipeline communication, and dehydrogenation tower (1) is communicated with by piping loop with First Heat Exchanger (4), and the first flash tank (6) is successively through First Heat Exchanger (4), second interchanger (5), pressure swing adsorber (8), second pressure charging valve (18), second interchanger (5), First Heat Exchanger (4), first flash tank (6) is communicated with piping loop, and the first flash tank (6) is successively through second throttle (18), First Heat Exchanger (4) is communicated with dehydrogenation tower (1) with pipeline, First Heat Exchanger (4) and the second interchanger (5) are with pipeline communication, second interchanger (5) circulates with the 3rd pressure charging valve (15) and is communicated with, denitrification column (2) is communicated with by piping loop with the 5th interchanger (11), denitrification column (2) and the 3rd interchanger (9) with pipeline communication, the second interchanger (5) successively with decompressor (16), 5th interchanger (11), 4th throttling valve (20), 3rd interchanger (9), second interchanger (5) with pipeline formed circulation be communicated with, the second interchanger (5) successively with decompressor (16), 6th interchanger (12), 4th interchanger (10), second interchanger (5) is formed circulation with pipeline and is communicated with.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420609821.0U CN204125172U (en) | 2014-10-22 | 2014-10-22 | Nitrogen cycle technique produces the system of CO |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420609821.0U CN204125172U (en) | 2014-10-22 | 2014-10-22 | Nitrogen cycle technique produces the system of CO |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204125172U true CN204125172U (en) | 2015-01-28 |
Family
ID=52381546
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420609821.0U Withdrawn - After Issue CN204125172U (en) | 2014-10-22 | 2014-10-22 | Nitrogen cycle technique produces the system of CO |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204125172U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326472A (en) * | 2014-10-22 | 2015-02-04 | 杭州中泰深冷技术股份有限公司 | System and method for preparing CO by nitrogen circulation process |
-
2014
- 2014-10-22 CN CN201420609821.0U patent/CN204125172U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326472A (en) * | 2014-10-22 | 2015-02-04 | 杭州中泰深冷技术股份有限公司 | System and method for preparing CO by nitrogen circulation process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103697659B (en) | The device and method of liquefied natural gas and rich hydrogen production is produced from high methane gas | |
| CN100472159C (en) | Air separating device and method therefor | |
| CN204115392U (en) | With the full air separation units producing liquids of air supply compressor | |
| CN103175381B (en) | Low concentration coal-bed gas produces LNG technique containing oxygen cryogenic liquefying | |
| CN102374754A (en) | Equipment and method for preparing liquid natural gas and carbon oxide from coke oven gas | |
| CN104326472B (en) | A kind of nitrogen cycle technique produces system and the method thereof of CO | |
| CN102435045A (en) | Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof | |
| CN103697661B (en) | The device and method of liquefied natural gas and rich hydrogen production is produced from coke-stove gas | |
| CN103175380B (en) | Low concentration coal-bed gas produces LNG device containing oxygen cryogenic liquefying | |
| CN102735020B (en) | Method for extracting helium from natural gas | |
| CN205373261U (en) | Low positive pressure of low high extraction percentage of liquid flows large -scale interior compression air separation system of inflation | |
| CN208536494U (en) | Skid-mounted type Internal-compression flow air separation plant | |
| CN102653692B (en) | Method for preparing liquefied natural gas from coke oven gas | |
| CN110553464A (en) | CO cryogenic separation system and method for reducing nitrogen circulation energy consumption | |
| CN204508803U (en) | The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide | |
| CN104729233B (en) | Natural gas liquefaction system with combination of auto-cascade refrigeration system and pulse tube refrigerator | |
| CN204125172U (en) | Nitrogen cycle technique produces the system of CO | |
| CN104190200B (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN203837413U (en) | Device for extracting ethane and hydrocarbon mixture from natural gas | |
| CN202246578U (en) | Composite refrigerant refrigerated light secondary-dealkylation hydrocarbon recovering device | |
| CN104495751A (en) | Method and device for preparing hydrogen and carbon monoxide by efficient synthesis gas separation | |
| CN202382518U (en) | Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas) | |
| CN203240840U (en) | Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station | |
| CN203487118U (en) | Device for recovering tail gas to prepare liquefied natural gas | |
| CN102141337A (en) | Method for separating air |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20150128 Effective date of abandoning: 20151230 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |