CN203687517U - Device for preparing LNG and hydrogen-rich products by utilizing methane-rich gas - Google Patents
Device for preparing LNG and hydrogen-rich products by utilizing methane-rich gas Download PDFInfo
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Abstract
The utility model relates to a device for preparing LNG and hydrogen-rich products by utilizing methane-rich gas. The device comprises a main heat exchanger, a mixed refrigerant compressor refrigeration system, a denitrifying rectification tower and a dehydrogenizing rectification tower. The device for preparing the LNG and hydrogen-rich products by utilizing the methane-rich gas adopts a three-section plate type mixed rectification + double-rectification-tower process, and the cooling capacity required by double rectification towers is provided by an ultra-low-temperature heat exchanger. Due to the fact that a low-temperature refrigerant separating tank is arranged behind a medium-temperature heat exchanger, the content of isopentane or iso-butane and other components in a separated mixed refrigerant is very low, and the channel blockage of the ultra-low-temperature heat exchanger is effectively avoided. The process is a single mixed refrigerant compressor refrigeration process, investment for one refrigerant compressor is saved, and the content of the isopentane or iso-butane in the mixed refrigerant proportioning is improved compared with the content in a two-section plate type process. Compared with two traditional mixed refrigerant compressors, the device is low in rectification process energy consumption, simple in operation and high in operation reliability.
Description
Technical field
The utility model relates to a kind of device of producing LNG and rich hydrogen production from high methane 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.
Because hydrogen content in methane-rich gas is higher, the separation temperature that liquefies is accordingly lower, thereby produces LNG and need consume lower cold compared with conventional gas.In traditional high methane gas, LNG processed and hydrogen-rich gas device adopt two cryogen compressors, on a hybrid refrigeration compressor foundation, increase again a nitrogen or nitrogen+methane blended Alternative Refrigerant Compressors, in, the pre-cold-peace liquefaction institute chilling requirement of the popular stock medium of low-temperature zone is provided by azeotrope compressor, rectifying column tower top condenser institute chilling requirement is provided by nitrogen or nitrogen+methane blended Alternative Refrigerant Compressors, although having avoided the component such as isopentane or iso-butane solidifies and then the problem of blocking plate fin heat exchanger passage in profound hypothermia section, but but because increased a nitrogen compressor, equipment investment increases, a unit of many operations, fault rate increases, operation easier increases, and energy consumption is higher.
Application number is 201210065876.5, name is called from high methane gas dehydrogenation nitrogen and produce the technique of liquefied natural gas and the Chinese patent of device, application number is 201110291609.5, name is called dehydrogenation from high methane gas, nitrogen, carbon monoxide and produces the Chinese patent of the technique of liquefied natural gas, these prior aries are at still Shortcomings of aspect such as refrigeration, high methane 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 LNG and rich hydrogen production from high methane gas that cost is low is provided.
The technical scheme in the invention for solving the above technical problem is:
From high methane gas, produce a device for LNG and rich hydrogen production, comprise main heat exchanger, azeotrope compressor refrigeration system, denitrogenation rectifying column, dehydrogenation rectifying column; Main heat exchanger is provided with mid temperature heat exchanger, cryogenic heat exchanger, profound hypothermia heat exchanger; In azeotrope compressor refrigeration system, be provided with hybrid refrigeration compressor and knockout drum; At the bottom of the tower of denitrogenation rectifying column, be provided with reboiler, tower top is provided with separator No. one; Dehydrogenation rectifying column tower top is provided with separator No. two;
The charging aperture of hybrid refrigeration compressor outlet and knockout drum is connected; The cold fluid section of the liquid outlet of knockout drum, the hot fluid section of mid temperature heat exchanger, mid temperature heat exchanger is connected successively, and the charging aperture of the gas vent of knockout drum, the hot fluid section of mid temperature heat exchanger, cryogenic coolant knockout drum is connected successively; The cold fluid section of the liquid outlet of cryogenic coolant knockout drum, the hot fluid section of cryogenic heat exchanger, cryogenic heat exchanger is connected successively, and the hot fluid section of the gas vent of cryogenic coolant knockout drum, the hot fluid section of cryogenic heat exchanger, profound hypothermia heat exchanger, the cold fluid section of profound hypothermia heat exchanger, the cold fluid section of cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively; The cold fluid section of mid temperature heat exchanger and hybrid refrigeration suction port of compressor are connected; This part structure has formed the recycle circuit of mix refrigerant;
The hot media channel of the hot fluid section of mid temperature heat exchanger, the hot fluid section of cryogenic heat exchanger, reboiler, the hot fluid section of profound hypothermia heat exchanger, the charging aperture of dehydrogenation rectifying column are connected successively; The charging aperture of the gas vent of dehydrogenation rectifying column, the hot fluid section of profound hypothermia heat exchanger, No. two separators is connected successively; The phegma entrance of the liquid outlet of No. two separators and dehydrogenation rectifying column is connected, and the cold fluid section of the gas vent of No. two separators, the cold fluid section of profound hypothermia heat exchanger, cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively; The charging aperture of the liquid outlet at the bottom of dehydrogenation rectifying tower and denitrogenation rectifying column is connected; Liquid outlet at the bottom of denitrogenation rectifying tower and the charging aperture of reboiler are connected, and the cold fluid section of the discharging opening of reboiler and profound hypothermia heat exchanger is connected; The charging aperture of the gas vent of denitrogenation rectifying column, the cold fluid section of profound hypothermia heat exchanger, a separator is connected successively; The phegma entrance of the liquid outlet of a separator and denitrogenation rectifying column is connected, and the cold fluid section of the gas vent of a separator, the cold fluid section of profound hypothermia heat exchanger, cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively; This part structure has formed high methane gas liquefaction and split circuit.
Mid temperature heat exchanger described in the utility model, cryogenic heat exchanger, profound hypothermia heat exchanger are plate-fin heat exchanger.
The utility model compared with prior art, has the following advantages and effect:
1, the utility model adopts three sections of board-like hybrid refrigeration+double rectification column techniques, two-tower rectification institute chilling requirement is provided by profound hypothermia heat exchanger, due to cryogenic coolant knockout drum being set after mid temperature heat exchanger, ensure that in the azeotrope after separating, the constituent content such as isopentane or iso-butane is very low, effectively avoided the problem of stopping up in profound hypothermia heat exchanger channel.Therefore technique described in the utility model is for adopting single mixed working fluid compressor cooling technique, having reduced in the investment of a cryogen compressor and azeotrope proportioning isopentane or iso-butane content can be greatly improved compared with two sections of board-like flow processs, low with two traditional azeotrope compressor cooling flow process energy consumptions, and simple to operate, operational reliability improves, energy consumption of unit product is low.
2, due to the variation of component in high methane gas, the required minimum temperature cold of rectifying can change to some extent, the utility model adopts the adjustment azeotrope proportioning that three sections of board-like mixed refrigeration process can be in a big way, to reduce the unit product required energy consumption that liquefies, can ensure that profound hypothermia heat exchanger channel there will not be blockage problem simultaneously.
Brief description of the drawings
Fig. 1 is the structural representation of the utility model embodiment.
Detailed description of the invention
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, the utility model is produced the equipment of LNG and rich hydrogen production from high methane gas, comprises main heat exchanger, azeotrope compressor refrigeration system 4, denitrogenation rectifying column 6, dehydrogenation rectifying column 9.The utility model is produced the method for LNG and rich hydrogen production from high methane gas, comprises azeotrope cyclic process, high methane gas liquefaction and separation process.
Main heat exchanger is provided with mid temperature heat exchanger 1, cryogenic heat exchanger 2, profound hypothermia heat exchanger 3 these three sections of plate-fin heat exchangers.
In azeotrope compressor refrigeration system 4, be provided with hybrid refrigeration compressor 11 and knockout drum 12.
At the bottom of the tower of denitrogenation rectifying column 6, be provided with reboiler 7, tower top is provided with separator 8 No. one.
Dehydrogenation rectifying column 9 tower tops are provided with separator 10 No. two.
High methane gas liquefaction and split circuit: the hot media channel of the hot fluid section of mid temperature heat exchanger 1, the hot fluid section of cryogenic heat exchanger 2, reboiler 7, the hot fluid section of profound hypothermia heat exchanger 3, the charging aperture of dehydrogenation rectifying column 9 are connected successively; The charging aperture of the gas vent of dehydrogenation rectifying column 9, the hot fluid section of profound hypothermia heat exchanger 3, No. two separators 10 is connected successively; The phegma entrance of the liquid outlet of No. two separators 10 and dehydrogenation rectifying column 9 is connected, and the cold fluid section of the gas vent of No. two separators 10, the cold fluid section of profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, the cold fluid section of mid temperature heat exchanger 1 are connected successively; Liquid outlet at the bottom of dehydrogenation rectifying column 9 towers and the charging aperture of denitrogenation rectifying column 6 are connected; Liquid outlet at the bottom of denitrogenation rectifying column 6 towers and the charging aperture of reboiler 7 are connected, and the cold fluid section of the discharging opening of reboiler 7 and profound hypothermia heat exchanger 3 is connected; The charging aperture of the gas vent of denitrogenation rectifying column 6, the cold fluid section of profound hypothermia heat exchanger 3, a separator 8 is connected successively; The phegma entrance of the liquid outlet of a separator 8 and denitrogenation rectifying column 6 is connected, and the cold fluid section of the gas vent of a separator 8, the cold fluid section of profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, the cold fluid section of mid temperature heat exchanger 1 are connected successively.
High methane gas liquefaction and separation process: the high methane gas after purification is sent into main heat exchanger by pipeline, pass through successively mid temperature heat exchanger 1 and cryogenic heat exchanger 2, the low pressure azeotrope being backflowed is cooled to enter after-105～-125 DEG C the reboiler 7 of denitrogenation rectifying column 6, as the thermal source of reboiler 7, simultaneously further cooling by the liquid of reboiler 7, after this return to profound hypothermia heat exchanger 3 and backflowed and after azeotrope is cooled to-135～-155 DEG C, enter dehydrogenation rectifying column 9 middle parts and carry out rectifying; Dehydrogenation rectifying column 9 overhead gas enter profound hypothermia heat exchanger 3 by pipeline, are further cooled to-165～-175 DEG C, then carry out gas-liquid separation by No. two separators 10 that pipeline enters dehydrogenation rectifying column 9 tower tops; No. two isolated liquid of separator 10 return to the rectifying that dehydrogenation rectifying column 9 is rectifying column as phegma provides cold, after isolated gas throttling, return to main heat exchanger, be recovered cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich hydrogen production.Liquid at the bottom of dehydrogenation rectifying column 9 towers is sent into 6 rectifying of denitrogenation rectifying column after throttling, after rectifying, at the bottom of denitrogenation rectifying column 6 towers, distillate is the LNG of-135～-145 DEG C, at the bottom of tower, distillate returns to profound hypothermia heat exchanger 3 and was chilled to-160～-170 DEG C, sends into LNG storage tank after throttling; The nitrogen-rich gas of denitrogenation rectifying column 6 tower tops returns to profound hypothermia heat exchanger 3 and is cooled to-165～-175 DEG C, enter a separator 8 by pipeline again and carry out gas-liquid separation, isolated liquid returns to the rectifying that denitrogenation rectifying column 6 is rectifying column as phegma cold is provided, isolated gas returns to main heat exchanger, reclaim cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich nitrogen product.
Azeotrope recycle circuit: 11 outlets of hybrid refrigeration compressor are connected with the charging aperture of knockout drum 12; The cold fluid section of the liquid outlet of knockout drum 12, the hot fluid section of mid temperature heat exchanger 1, mid temperature heat exchanger 1 is connected successively, and the charging aperture of the gas vent of knockout drum 12, the hot fluid section of mid temperature heat exchanger 1, cryogenic coolant knockout drum 5 is connected successively; The cold fluid section of the liquid outlet of cryogenic coolant knockout drum 5, the hot fluid section of cryogenic heat exchanger 2, cryogenic heat exchanger 2 is connected successively, and the hot fluid section of the gas vent of cryogenic coolant knockout drum 5, the hot fluid section of cryogenic heat exchanger 2, profound hypothermia heat exchanger 3, the cold fluid section of profound hypothermia heat exchanger 3, the cold fluid section of cryogenic heat exchanger 2, the cold fluid section of mid temperature heat exchanger 1 are connected successively; The cold fluid section of mid temperature heat exchanger 1 and hybrid refrigeration compressor 11 entrances are connected.
Azeotrope cyclic process: enter hybrid refrigeration compressor 11 after azeotrope cooling box, cooled azeotrope is divided into gas, liquid two-phase cryogen through knockout drum 12, gas, that liquid two-phase cryogen enters mid temperature heat exchanger 1 by pipeline is respectively cooling; Mid temperature heat exchanger 1 is returned in the throttling after mid temperature heat exchanger 1 is cooling of liquid phase cryogen provides cold; Gas phase cryogen enters cryogenic coolant knockout drum 5 by pipeline after mid temperature heat exchanger 1 is cooling, after cryogenic coolant knockout drum 5 is divided into gas, liquid two fluid streams, enters cryogenic heat exchanger 2 respectively by pipeline; Wherein cryogenic heat exchanger 2 is returned in liquid phase fluid throttling after cryogenic heat exchanger 2 is cooling provides cold, gas phase cryogen fluid, after cryogenic heat exchanger 2 is cooling, then enters the further cooling rear throttling of profound hypothermia heat exchanger 3 by pipeline and returns to successively profound hypothermia heat exchanger 3 and cryogenic heat exchanger 2 and provide cold for heat exchanger; Multiply azeotrope fluid after cryogenic heat exchanger 2 and 3 heat exchange of profound hypothermia heat exchanger, before mid temperature heat exchanger 1, merge into a fluid streams and enter mid temperature heat exchanger 1 by pipeline, for mid temperature heat exchanger 1 provides cold again, finally return to azeotrope compressor 11 entrances, compression again, forms azeotrope circulation.
The azeotrope of said process is mixed by methane, ethene, propane, isopentane, nitrogen or methane, ethene, propane, iso-butane, nitrogen.
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.
Embodiment 1:
Azeotrope is mixed by methane, ethene, propane, isopentane and nitrogen.Azeotrope cyclic process: enter hybrid refrigeration compressor 11 after azeotrope cooling box under 0.25MPa, be compressed into 3.8MPa and cooling after enter knockout drum 12 and be divided into gas, liquid two-phase cryogen, gas, liquid two-phase cryogen enter mid temperature heat exchanger 1 by pipeline respectively and are cooled to-40 DEG C; Mid temperature heat exchanger 1 is returned in the throttling after mid temperature heat exchanger 1 is cooling of liquid phase cryogen provides cold; Gas phase cryogen enters cryogenic coolant knockout drum 5 by pipeline after mid temperature heat exchanger 1 is cooling, after cryogenic coolant knockout drum 5 is divided into gas, liquid two fluid streams, enters cryogenic heat exchanger 2 respectively by pipeline; Wherein cryogenic heat exchanger 2 is returned in liquid phase fluid throttling after cryogenic heat exchanger 2 is cooling provides cold, gas phase cryogen fluid, after cryogenic heat exchanger 2 is cooling, then enters profound hypothermia heat exchanger 3 by pipeline and is further cooled to-172 DEG C, is throttled to and returns to successively profound hypothermia heat exchanger 3 and cryogenic heat exchanger 2 after 0.3MPa and provide cold for heat exchanger; Multiply azeotrope fluid after cryogenic heat exchanger 2 and 3 heat exchange of profound hypothermia heat exchanger, before mid temperature heat exchanger 1, merge into a fluid streams and enter mid temperature heat exchanger 1 by pipeline, for mid temperature heat exchanger 1 provides cold again, after rewarming to 37 DEG C, finally return to azeotrope compressor 11 entrances, compression again, forms azeotrope circulation.
Embodiment 2:
Azeotrope is mixed by methane, ethene, propane, iso-butane and nitrogen.Azeotrope cyclic process: enter hybrid refrigeration compressor 11 after azeotrope cooling box under 0.20MPa, be compressed into 3.4MPa and cooling after enter knockout drum 12 and be divided into gas, liquid two-phase cryogen, gas, liquid two-phase cryogen enter mid temperature heat exchanger 1 by pipeline respectively and are cooled to-50 DEG C; Mid temperature heat exchanger 1 is returned in the throttling after mid temperature heat exchanger 1 is cooling of liquid phase cryogen provides cold; Gas phase cryogen enters cryogenic coolant knockout drum 5 by pipeline after mid temperature heat exchanger 1 is cooling, after cryogenic coolant knockout drum 5 is divided into gas, liquid two fluid streams, enters cryogenic heat exchanger 2 respectively by pipeline; Wherein cryogenic heat exchanger 2 is returned in liquid phase fluid throttling after cryogenic heat exchanger 2 is cooling provides cold, gas phase cryogen fluid, after cryogenic heat exchanger 2 is cooling, then enters profound hypothermia heat exchanger 3 by pipeline and is further cooled to-173 DEG C, is throttled to and returns to successively profound hypothermia heat exchanger 3 and cryogenic heat exchanger 2 after 0.27MPa and provide cold for heat exchanger; Multiply azeotrope fluid after cryogenic heat exchanger 2 and 3 heat exchange of profound hypothermia heat exchanger, before mid temperature heat exchanger 1, merge into a fluid streams and enter mid temperature heat exchanger 1 by pipeline, for mid temperature heat exchanger 1 provides cold again, after rewarming to 37 DEG C, finally return to azeotrope compressor 11 entrances, compression again, forms azeotrope circulation.
Embodiment 3:
High methane gas liquefaction and separation process: the high methane gas after purification is sent into main heat exchanger by pipeline, pass through successively mid temperature heat exchanger 1 and cryogenic heat exchanger 2, the low pressure azeotrope being backflowed is cooled to enter after-120 DEG C the reboiler 7 of denitrogenation rectifying column 6, as the thermal source of reboiler 7, simultaneously further cooling by the liquid of reboiler 7, after this return to profound hypothermia heat exchanger 3 and backflowed and after azeotrope is cooled to-155 DEG C, enter dehydrogenation rectifying column 9 middle parts and carry out rectifying; Dehydrogenation rectifying column 9 overhead gas enter profound hypothermia heat exchanger 3 by pipeline, are further cooled to-172 DEG C, then carry out gas-liquid separation by No. two separators 10 that pipeline enters dehydrogenation rectifying column 9 tower tops; No. two isolated liquid of separator 10 return to the rectifying that dehydrogenation rectifying column 9 is rectifying column as phegma provides cold, after isolated gas throttling, return to main heat exchanger, be recovered cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich hydrogen production.Liquid at the bottom of dehydrogenation rectifying column 9 towers is sent into 6 rectifying of denitrogenation rectifying column after throttling, and after rectifying, at the bottom of denitrogenation rectifying column 6 towers, distillate is the LNG of-140 DEG C, and at the bottom of tower, distillate returns to profound hypothermia heat exchanger 3 and was chilled to-163 DEG C, sends into LNG storage tank after throttling; The nitrogen-rich gas of denitrogenation rectifying column 6 tower tops returns to profound hypothermia heat exchanger 3 and is cooled to-172 DEG C, enter a separator 8 by pipeline again and carry out gas-liquid separation, isolated liquid returns to the rectifying that denitrogenation rectifying column 6 is rectifying column as phegma cold is provided, isolated gas returns to main heat exchanger, reclaim cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich nitrogen product.
Embodiment 4:
High methane gas liquefaction and separation process: the high methane gas after purification is sent into main heat exchanger by pipeline, pass through successively mid temperature heat exchanger 1 and cryogenic heat exchanger 2, the low pressure azeotrope being backflowed is cooled to enter after-120 DEG C the reboiler 7 of denitrogenation rectifying column 6, as the thermal source of reboiler 7, simultaneously further cooling by the liquid of reboiler 7, after this return to profound hypothermia heat exchanger 3 and backflowed and after azeotrope is cooled to-150 DEG C, enter dehydrogenation rectifying column 9 middle parts and carry out rectifying; Dehydrogenation rectifying column 9 overhead gas enter profound hypothermia heat exchanger 3 by pipeline, are further cooled to-172 DEG C, then carry out gas-liquid separation by No. two separators 10 that pipeline enters dehydrogenation rectifying column 9 tower tops; No. two isolated liquid of separator 10 return to the rectifying that dehydrogenation rectifying column 9 is rectifying column as phegma provides cold, after isolated gas throttling, return to main heat exchanger, be recovered cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich hydrogen production.Liquid at the bottom of dehydrogenation rectifying column 9 towers is sent into 6 rectifying of denitrogenation rectifying column after throttling, and after rectifying, at the bottom of denitrogenation rectifying column 6 towers, distillate is the LNG of-140 DEG C, and at the bottom of tower, distillate returns to profound hypothermia heat exchanger 3 and was chilled to-163 DEG C, sends into LNG storage tank after throttling; The nitrogen-rich gas of denitrogenation rectifying column 6 tower tops returns to profound hypothermia heat exchanger 3 and is cooled to-172 DEG C, enter a separator 8 by pipeline again and carry out gas-liquid separation, isolated liquid returns to the rectifying that denitrogenation rectifying column 6 is rectifying column as phegma cold is provided, isolated gas returns to main heat exchanger, reclaim cold through profound hypothermia heat exchanger 3, cryogenic heat exchanger 2, mid temperature heat exchanger 1 successively, after rewarming, return as rich nitrogen product.
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 LNG and rich hydrogen production from high methane gas, is characterized in that: comprise main heat exchanger, azeotrope compressor refrigeration system, denitrogenation rectifying column, dehydrogenation rectifying column; Main heat exchanger is provided with mid temperature heat exchanger, cryogenic heat exchanger, profound hypothermia heat exchanger; In azeotrope compressor refrigeration system, be provided with hybrid refrigeration compressor and knockout drum; At the bottom of the tower of denitrogenation rectifying column, be provided with reboiler, tower top is provided with separator No. one; Dehydrogenation rectifying column tower top is provided with separator No. two;
The charging aperture of hybrid refrigeration compressor outlet and knockout drum is connected; The cold fluid section of the liquid outlet of knockout drum, the hot fluid section of mid temperature heat exchanger, mid temperature heat exchanger is connected successively, and the charging aperture of the gas vent of knockout drum, the hot fluid section of mid temperature heat exchanger, cryogenic coolant knockout drum is connected successively; The cold fluid section of the liquid outlet of cryogenic coolant knockout drum, the hot fluid section of cryogenic heat exchanger, cryogenic heat exchanger is connected successively, and the hot fluid section of the gas vent of cryogenic coolant knockout drum, the hot fluid section of cryogenic heat exchanger, profound hypothermia heat exchanger, the cold fluid section of profound hypothermia heat exchanger, the cold fluid section of cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively; The cold fluid section of mid temperature heat exchanger and hybrid refrigeration suction port of compressor are connected;
The hot media channel of the hot fluid section of mid temperature heat exchanger, the hot fluid section of cryogenic heat exchanger, reboiler, the hot fluid section of profound hypothermia heat exchanger, the charging aperture of dehydrogenation rectifying column are connected successively; The charging aperture of the gas vent of dehydrogenation rectifying column, the hot fluid section of profound hypothermia heat exchanger, No. two separators is connected successively; The phegma entrance of the liquid outlet of No. two separators and dehydrogenation rectifying column is connected, and the cold fluid section of the gas vent of No. two separators, the cold fluid section of profound hypothermia heat exchanger, cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively; The charging aperture of the liquid outlet at the bottom of dehydrogenation rectifying tower and denitrogenation rectifying column is connected; Liquid outlet at the bottom of denitrogenation rectifying tower and the charging aperture of reboiler are connected, and the cold fluid section of the discharging opening of reboiler and profound hypothermia heat exchanger is connected; The charging aperture of the gas vent of denitrogenation rectifying column, the cold fluid section of profound hypothermia heat exchanger, a separator is connected successively; The phegma entrance of the liquid outlet of a separator and denitrogenation rectifying column is connected, and the cold fluid section of the gas vent of a separator, the cold fluid section of profound hypothermia heat exchanger, cryogenic heat exchanger, the cold fluid section of mid temperature heat exchanger are connected successively.
2. the device of producing LNG and rich hydrogen production from high methane gas according to claim 1, is characterized in that: described mid temperature heat exchanger, cryogenic heat exchanger, profound hypothermia heat exchanger are plate-fin heat exchanger.
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| CN201320852867.0U CN203687517U (en) | 2013-12-23 | 2013-12-23 | Device for preparing LNG and hydrogen-rich products by utilizing methane-rich gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN107024074A (en) * | 2017-05-19 | 2017-08-08 | 河南开元空分集团有限公司 | A kind of nitrogen single-stage expansion refrigeration reclaims methane in methanol-fueled CLC tail gas for LNG devices and methods therefor |
-
2013
- 2013-12-23 CN CN201320852867.0U patent/CN203687517U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN107024074A (en) * | 2017-05-19 | 2017-08-08 | 河南开元空分集团有限公司 | A kind of nitrogen single-stage expansion refrigeration reclaims methane in methanol-fueled CLC tail gas for LNG devices and methods therefor |
| CN107024074B (en) * | 2017-05-19 | 2022-08-16 | 河南开元空分集团有限公司 | Device and method for preparing LNG (liquefied Natural gas) by recovering methane in methanol synthesis tail gas through nitrogen single-stage expansion refrigeration |
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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. |
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Granted publication date: 20140702 Termination date: 20171223 |