CN203687516U - Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas - Google Patents
Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas Download PDFInfo
- Publication number
- CN203687516U CN203687516U CN201320852819.1U CN201320852819U CN203687516U CN 203687516 U CN203687516 U CN 203687516U CN 201320852819 U CN201320852819 U CN 201320852819U CN 203687516 U CN203687516 U CN 203687516U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- gas
- fluid section
- liquid
- liquefaction
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to a device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas. The device comprises a mixed refrigerant compressor refrigeration system, a precooling system and a liquidation cold box system. The device adopts a single-mixed-refrigerant and single-tower rectification process and only can adopts one refrigerant compressor and one rectification tower. Compared with an existing coke oven gas separation liquefaction device including two refrigerant compressors and two rectification towers, the device investment cost and the system energy consumption are reduced, and starting and stopping operations are convenient and quick. Considering overall economic efficiency, the device is suitable for a liquidation device (<=1000,000 squares/per day of purified coke oven gas) with high purified coke oven gas pressure (>=2.3MPa) and small coke oven gas processing scale and is less in device investment, low in unit energy consumption and simple in operation.
Description
Technical field
The utility model relates to a kind of device of producing liquefied natural gas and rich hydrogen production from coke-stove gas.
Background technology
Enriched Gas comparatively commonly coke-stove gas improves calorific value by methanation reaction, make most carbon monoxide, carbon dioxide conversion become methane, the methane volume fraction that the synthesis gas of gained obtains after the purification after naphthalene, desulfurization are washed in water washing de-oiling is again more than 40～50%, is separately rich in hydrogen and nitrogen.High methane gas is prepared LNG and rich hydrogen production through low-temperature liquefaction, cryogenic rectification again.The coke-stove gas that is the richest in alkanisation through purifying, liquefaction separates the problem of preparing liquefied natural gas and not only can alleviate domestic natural gas shortage, and can promote technological progress and the industry development of coking and energy industry, development coke-stove gas LNG project processed can produce obvious economic benefit, environmental benefit and social benefit, coke-stove gas is recycled to industry significant.
High methane gas and conventional gas composition has larger difference, and nitrogen, hydrogen content are relatively high, therefore liquefaction and separating technology is more complicated, energy consumption of unit product is higher.
The existing technique of producing liquefied natural gas and rich hydrogen production from coke-stove gas, comprises two cryogen compressors and two rectifying columns, and equipment investment is large, and energy consumption is high.
Application number is 200810135211.0, name is called the separating technology of preparing liquefied natural gas from coke oven gas and the Chinese patent of equipment, application number is 201010592131.5, name is called a kind of Chinese patent of being produced the method for liquefied natural gas by coke-stove gas, these prior aries are at still Shortcomings of aspect such as refrigeration, coke-stove gas liquefaction and separating effects, specific energy consumption is higher, and hydrogen-rich gas is produced to deficiency, easily cause waste.
Utility model content
The purpose of this utility model is to overcome above shortcomings in prior art, and a kind of reasonable in design, energy-conservation, device of producing liquefied natural gas and rich hydrogen production from coke-stove gas that cost is low is provided.
The technical scheme in the invention for solving the above technical problem is:
From coke-stove gas, produce a device for liquefied natural gas and rich hydrogen production, comprise azeotrope compressor refrigeration system, chilldown system, liquefaction ice chest system; Described azeotrope compressor refrigeration system comprises azeotrope compressor, intercooler, aftercooler, middle knockout drum; Azeotrope compressor has one section of compression and compresses two sections; Described chilldown system comprises precool heat exchanger device, cryogen gas-liquid separator; Described liquefaction ice chest system comprises cooling heat exchanger, liquefaction heat exchanger, dehydrogenation liquid/gas separator, is provided with the denitrogenation rectifying column of tower bottom reboiler and tower overhead gas liquid/gas separator;
Two sections of the compressions of one section of the compression of azeotrope compressor, intercooler, middle knockout drum, azeotrope compressor, aftercooler, the hot fluid section of precool heat exchanger device, the compound import of cryogen gas-liquid separator are connected successively; The hot fluid section of the gas vent of cryogen gas-liquid separator, the hot fluid section of cooling heat exchanger, liquefaction heat exchanger, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger are connected successively; The cold fluid section of the liquid outlet of cryogen gas-liquid separator, the hot fluid section of cooling heat exchanger, cooling heat exchanger is connected successively; The cold fluid section of cooling heat exchanger and one section of connection of the compression of azeotrope compressor; This part structure has formed the recycle circuit of azeotrope;
Hot fluid section, the tower bottom reboiler of the hot fluid section of precool heat exchanger device, the hot fluid section of cooling heat exchanger, liquefaction heat exchanger are connected successively; The compound import of dehydrogenation liquid/gas separator and tower bottom reboiler are connected, the charging aperture of liquid outlet and denitrogenation rectifying column is connected, and the gas vent of dehydrogenation liquid/gas separator, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger, the cold fluid section of precool heat exchanger device are connected successively; The tower top of denitrogenation rectifying column, the hot fluid section of liquefaction heat exchanger, the charging aperture of tower overhead gas liquid/gas separator are connected successively; The gas vent of tower overhead gas liquid/gas separator, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger, the cold fluid section of precool heat exchanger device are connected successively; The phegma entrance of the liquid outlet of tower overhead gas liquid/gas separator and denitrogenation rectifying column is connected; At the bottom of the tower of denitrogenation rectifying column, connect with the hot fluid section of liquefaction heat exchanger; The circuit that this part structure has formed coke-stove gas liquefaction and separated.
Precool heat exchanger device described in the utility model, cooling heat exchanger, liquefaction heat exchanger are plate-fin heat exchanger.
The utility model compared with prior art, have the following advantages and effect: the utility model adopts single hybrid refrigeration and single tower distillation flow process, can only adopt a cryogen compressor and a rectifying column, compare with the existing coke-stove gas parting liquid gasifying device that comprises two cryogen compressors and two rectifying columns, the energy consumption of equipment investment expense and system all reduces, and start-stop car simple operation, consider from overall economic efficiency, this device is suitable for purifying rear coke-stove gas pressure higher (>=2.3MPa), the liquefying plant (≤100 ten thousand mark side/sky purifying coke oven gas) that coke-stove gas treatment scale is little, equipment investment is few, specific energy consumption is lower, operate simpler.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model embodiment.
The specific embodiment
Below in conjunction with accompanying drawing and by embodiment, the utility model is described in further detail, and following examples are to explanation of the present utility model and the utility model is not limited to following examples.
Referring to Fig. 1, from coke-stove gas, produce the device of liquefied natural gas and rich hydrogen production, comprise azeotrope compressor refrigeration system, chilldown system, liquefaction ice chest system, and connecting line between each system and equipment thereof.From coke-stove gas, produce the method for liquefied natural gas and rich hydrogen production, comprise azeotrope cyclic process and purifying coke oven gas liquefaction and separation process.
Azeotrope compressor refrigeration system comprises that motor drives or steam-powered azeotrope compressor 1, intercooler 2, aftercooler 3, knockout drum 4 in the middle of.Azeotrope compressor 1 has one section of compression and compresses two sections.
Chilldown system comprises a precool heat exchanger device 5, a cryogen gas-liquid separator 11.
Liquefaction ice chest system comprises a cooling heat exchanger 6, liquefaction heat exchanger 7, dehydrogenation liquid/gas separator 9, a denitrogenation rectifying column 8 that is provided with tower bottom reboiler 10 and tower overhead gas liquid/gas separator 12.
Azeotrope recycle circuit: two sections of the compressions of one section of the compression of azeotrope compressor 1, intercooler 2, middle knockout drum 4, azeotrope compressor 1, aftercooler 3, the hot fluid section of precool heat exchanger device 5, the compound import of cryogen gas-liquid separator 11 are connected successively.The hot fluid section of the gas vent of cryogen gas-liquid separator 11, the hot fluid section of cooling heat exchanger 6, liquefaction heat exchanger 7, the cold fluid section of liquefaction heat exchanger 7, the cold fluid section of cooling heat exchanger 6 are connected successively.The cold fluid section of the liquid outlet of cryogen gas-liquid separator 11, the hot fluid section of cooling heat exchanger 6, cooling heat exchanger 6 is connected successively.The cold fluid section of cooling heat exchanger 6 and one section of connection of the compression of azeotrope compressor 1.
Azeotrope cyclic process: the mixed working fluid being made up of C1～C5 and nitrogen enters azeotrope compressor 1 entrance through rational proportion, compressed one section is compressed to and enters intercooler 2 after 0.8～1.3MPa and be cooled to 30～50 ℃, then in the middle of entering, knockout drum 4 carries out gas-liquid separation; The middle knockout drum 4 isolated gases in top continue to enter two sections of entrances of compression of azeotrope compressor 1, after two sections are compressed to 2.0～4.0MPa, enter again aftercooler 3 and be cooled to 30～50 ℃, enter again precool heat exchanger device 5 hot fluid sections and participate in heat exchange, be cooled to 5～12 ℃; Mixed working fluid after precooling enters and in cryogen gas-liquid separator 11, carries out gas-liquid separation, the hot fluid section that the gas that cryogen gas-liquid separator 11 top gas export out enters the cooling heat exchanger 6 of liquefaction ice chest participates in heat exchange, be chilled in advance the hot fluid section participation heat exchange that enters liquefaction heat exchanger 7 after-45～-75 ℃, be cooled to-155～-165 ℃, after throttling to 0.22 again～0.4MPa, return to the cold fluid section of liquefaction heat exchanger 7, for it provides cold by extremely-50～-80 ℃ of re-heats.The hot fluid section that the liquid outlet of cryogen gas-liquid separator 11 bottoms liquid out enters the cooling heat exchanger 6 of liquefaction ice chest as liquid phase cryogen participates in heat exchange, be cooled to therein-45～-75 ℃, the cold fluid section that the mixed working fluid stream strand returning with liquefaction heat exchanger 7 cold fluid sections after throttling to 0.20～0.38MPa converges merging and oppositely enters cooling heat exchanger 6, forms azeotrope circulation for it provides the one section of entrance compression of compression that enters again azeotrope compressor 1 behind cold re-heat to 5～12 ℃.
Coke-stove gas liquefaction and split circuit: hot fluid section, the tower bottom reboiler 10 of the hot fluid section of precool heat exchanger device 5, the hot fluid section of cooling heat exchanger 6, liquefaction heat exchanger 7 are connected successively.Compound import and the tower bottom reboiler 10 of dehydrogenation liquid/gas separator 9 are connected, the charging aperture of liquid outlet and denitrogenation rectifying column 8 is connected, and the gas vent of dehydrogenation liquid/gas separator 9, the cold fluid section of liquefaction heat exchanger 7, the cold fluid section of cooling heat exchanger 6, the cold fluid section of precool heat exchanger device 5 are connected successively.The tower top of denitrogenation rectifying column 8, the hot fluid section of liquefaction heat exchanger 7, the charging aperture of tower overhead gas liquid/gas separator 12 are connected successively.The gas vent of tower overhead gas liquid/gas separator 12, the cold fluid section of liquefaction heat exchanger 7, the cold fluid section of cooling heat exchanger 6, the cold fluid section of precool heat exchanger device 5 are connected successively; The phegma entrance of the liquid outlet of tower overhead gas liquid/gas separator 12 and denitrogenation rectifying column 8 is connected.At the bottom of the tower of denitrogenation rectifying column 8, connect with the hot fluid section of liquefaction heat exchanger 7.
Coke-stove gas liquefaction and separation process: the coke-stove gas after purification is chilled in advance through precool heat exchanger device 5 cooling heat exchanger 6 that enters liquefaction ice chest after 5～12 ℃ and is cooled to-45～-75 ℃, entering liquefaction heat exchanger 7 is cooled to and after the tower bottom reboiler 10 that enters denitrogenation rectifying column 8 after-117～-130 ℃ continues to be cooled to-130～-150 ℃, enters dehydrogenation liquid/gas separator 9 and carry out gas-liquid separation again, dehydrogenation liquid/gas separator 9 top isolated hydrogen content 85%(volumes) return to liquefaction heat exchanger 7 after above hydrogen-rich gas throttling to 0.6～0.7MPa, cooling heat exchanger 6, precool heat exchanger device 5 provides cold as cold strand for heat exchanger, the final rich hydrogen production of re-heat to 30～40 ℃ conduct.The liquid of dehydrogenation liquid/gas separator 9 bottoms is sent into 8 rectifying of denitrogenation rectifying column after throttling, denitrogenation rectifying column 8 tower tops gas out returns to liquefaction heat exchanger 7 and enters tower overhead gas liquid/gas separator 12 after continuing to be cooled to-160～-168 ℃ and carry out gas-liquid separation, the isolated nitrogen-rich gas in tower overhead gas liquid/gas separator 12 tops return liquefaction heat exchanger 7, cooling heat exchanger 6, precool heat exchanger device 5 as cold strand for heat exchanger provides cold, the final rich nitrogen product of re-heat to 30～40 ℃ conduct.The liquid of tower overhead gas liquid/gas separator 12 bottoms enters denitrogenation rectifying column 8, provides cold as the top low temperature reflux liquid of denitrogenation rectifying column 8 for 8 rectifying of denitrogenation rectifying column.The distillate of denitrogenation rectifying column 8 bottoms is-135～-145 ℃, methane content >=98%(volume) liquefied natural gas, liquefied natural gas return liquefaction heat exchanger 7 be chilled to-160～-170 ℃, after throttling, send into LNG storage tank stores.
Chilled brine circuit: the chilled brine of 5～9 ℃ from lithium bromide precooling unit provides cold as the cold thigh of precool heat exchanger device 5 for it, is gone out precool heat exchanger device 5 by re-heat to 7～12 ℃.
Fluid in the hot fluid section of above-described each heat exchanger receives cold, and temperature reduces; Fluid in cold fluid section provides cold, and temperature raises, the common practise that this concept is this area.
In addition, it should be noted that, the specific embodiment described in this description, shape, institute's title of being named etc. of its parts and components can be different, and the above content described in this description is only to the explanation of the utility model structure example.
Claims (2)
1. a device of producing liquefied natural gas and rich hydrogen production from coke-stove gas, is characterized in that: comprise azeotrope compressor refrigeration system, chilldown system, liquefaction ice chest system; Described azeotrope compressor refrigeration system comprises azeotrope compressor, intercooler, aftercooler, middle knockout drum; Azeotrope compressor has one section of compression and compresses two sections; Described chilldown system comprises precool heat exchanger device, cryogen gas-liquid separator; Described liquefaction ice chest system comprises cooling heat exchanger, liquefaction heat exchanger, dehydrogenation liquid/gas separator, is provided with the denitrogenation rectifying column of tower bottom reboiler and tower overhead gas liquid/gas separator;
Two sections of the compressions of one section of the compression of azeotrope compressor, intercooler, middle knockout drum, azeotrope compressor, aftercooler, the hot fluid section of precool heat exchanger device, the compound import of cryogen gas-liquid separator are connected successively; The hot fluid section of the gas vent of cryogen gas-liquid separator, the hot fluid section of cooling heat exchanger, liquefaction heat exchanger, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger are connected successively; The cold fluid section of the liquid outlet of cryogen gas-liquid separator, the hot fluid section of cooling heat exchanger, cooling heat exchanger is connected successively; The cold fluid section of cooling heat exchanger and one section of connection of the compression of azeotrope compressor;
Hot fluid section, the tower bottom reboiler of the hot fluid section of precool heat exchanger device, the hot fluid section of cooling heat exchanger, liquefaction heat exchanger are connected successively; The compound import of dehydrogenation liquid/gas separator and tower bottom reboiler are connected, the charging aperture of liquid outlet and denitrogenation rectifying column is connected, and the gas vent of dehydrogenation liquid/gas separator, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger, the cold fluid section of precool heat exchanger device are connected successively; The tower top of denitrogenation rectifying column, the hot fluid section of liquefaction heat exchanger, the charging aperture of tower overhead gas liquid/gas separator are connected successively; The gas vent of tower overhead gas liquid/gas separator, the cold fluid section of liquefaction heat exchanger, the cold fluid section of cooling heat exchanger, the cold fluid section of precool heat exchanger device are connected successively; The phegma entrance of the liquid outlet of tower overhead gas liquid/gas separator and denitrogenation rectifying column is connected; At the bottom of the tower of denitrogenation rectifying column, connect with the hot fluid section of liquefaction heat exchanger.
2. the device of producing liquefied natural gas and rich hydrogen production from coke-stove gas according to claim 1, is characterized in that: described precool heat exchanger device, cooling heat exchanger, liquefaction heat exchanger are plate-fin heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320852819.1U CN203687516U (en) | 2013-12-23 | 2013-12-23 | Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320852819.1U CN203687516U (en) | 2013-12-23 | 2013-12-23 | Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203687516U true CN203687516U (en) | 2014-07-02 |
Family
ID=51009404
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320852819.1U Expired - Fee Related CN203687516U (en) | 2013-12-23 | 2013-12-23 | Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203687516U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN104293402A (en) * | 2014-09-26 | 2015-01-21 | 成都赛普瑞兴科技有限公司 | Method of separating and purifying methane gas containing hydrogen gas and carbon monoxide to prepare liquefied natural gas |
-
2013
- 2013-12-23 CN CN201320852819.1U patent/CN203687516U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN104293402A (en) * | 2014-09-26 | 2015-01-21 | 成都赛普瑞兴科技有限公司 | Method of separating and purifying methane gas containing hydrogen gas and carbon monoxide to prepare liquefied natural gas |
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 | |
| CN104528647B (en) | The method and apparatus that a kind of synthesis gas separates hydrogen making and high-purity CO | |
| CN103697661B (en) | The device and method of liquefied natural gas and rich hydrogen production is produced from coke-stove gas | |
| CN202254637U (en) | Gas deep-cooling separated liquefying device for methanated coal gas | |
| CN108795508B (en) | Method for separating coke oven gas by utilizing expansion refrigeration of nitrogen and helium | |
| CN102353233B (en) | Process method and device for cryogenically separating and liquefying gas obtained after coal gas methanation | |
| CN103523751A (en) | Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen | |
| CN102435045A (en) | Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof | |
| CN210625119U (en) | CO cryogenic separation system capable of reducing nitrogen circulation energy consumption | |
| CN109019600A (en) | It is a kind of using multitower rectifying coproduction technical grade, the device and method of food-grade and high purity liquid carbon dioxide | |
| CN203513622U (en) | Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG) | |
| CN204508803U (en) | The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide | |
| CN203687516U (en) | Device for preparing liquefied natural gas and hydrogen-rich products by utilizing coke oven gas | |
| CN102519222A (en) | Cryogenic separation method for preparing liquefied natural gas from coke-oven gas | |
| CN202382517U (en) | Cryogenic separation system of using coke-oven gas to produce liquefied natural gas | |
| CN106871576B (en) | Commercial syngas low temperature front-end demethanization method and system | |
| CN103697660B (en) | The device and method of LNG and rich hydrogen production is produced from high methane gas | |
| CN201607093U (en) | Device for recovering liquefied carbon dioxide in petrochemical tail gas | |
| CN202382518U (en) | Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas) | |
| CN104495751A (en) | Method and device for preparing hydrogen and carbon monoxide by efficient synthesis gas separation | |
| CN206094746U (en) | Extract novel device of liquid methane in follow high methane gas | |
| CN204702504U (en) | A kind of synthetic gas is separated hydrogen making and high-purity CO device | |
| CN203837409U (en) | Device for preparing liquefied natural gas and hydrogen-rich products from methane-rich gas | |
| CN204693949U (en) | A kind of separation high methane gas device with n-formyl sarcolysine alkane refrigerating function | |
| CN201377962Y (en) | Equipment for preparing compressed natural gas from methane-containing mixed gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP02 | Change in the address of a patent holder |
Address after: 312400, Shaoxing, Zhejiang, Shengzhou Pukou street, 288 South Avenue, west two floor Patentee after: Zoko Energy Equipment Co., Ltd. Address before: 310051, room 1509, No. 2401 bin Sheng Road, Hangzhou, Zhejiang, Binjiang District Patentee before: Zoko Energy Equipment Co., Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140702 Termination date: 20171223 |