CN109420419A - A kind of decomposition of hydrate device, mixed gas separation system and separation method - Google Patents
A kind of decomposition of hydrate device, mixed gas separation system and separation method Download PDFInfo
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- CN109420419A CN109420419A CN201710715566.6A CN201710715566A CN109420419A CN 109420419 A CN109420419 A CN 109420419A CN 201710715566 A CN201710715566 A CN 201710715566A CN 109420419 A CN109420419 A CN 109420419A
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- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 147
- 238000000926 separation method Methods 0.000 title claims abstract description 76
- 239000002002 slurry Substances 0.000 claims abstract description 121
- 239000007788 liquid Substances 0.000 claims abstract description 108
- 238000000034 method Methods 0.000 claims abstract description 31
- 239000000463 material Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 154
- 239000012224 working solution Substances 0.000 claims description 47
- 238000006703 hydration reaction Methods 0.000 claims description 34
- 230000008929 regeneration Effects 0.000 claims description 33
- 238000011069 regeneration method Methods 0.000 claims description 33
- 230000036571 hydration Effects 0.000 claims description 32
- 239000012071 phase Substances 0.000 claims description 30
- 239000008246 gaseous mixture Substances 0.000 claims description 24
- 230000008569 process Effects 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 238000003860 storage Methods 0.000 claims description 19
- 238000005406 washing Methods 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 14
- 238000004140 cleaning Methods 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 11
- 238000012545 processing Methods 0.000 claims description 11
- 230000000694 effects Effects 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 8
- 230000004888 barrier function Effects 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 3
- 239000002283 diesel fuel Substances 0.000 claims description 2
- 239000003995 emulsifying agent Substances 0.000 claims description 2
- 239000003350 kerosene Substances 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 229920002545 silicone oil Polymers 0.000 claims description 2
- 239000000839 emulsion Substances 0.000 claims 1
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- 238000005265 energy consumption Methods 0.000 abstract description 11
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- 238000005516 engineering process Methods 0.000 description 11
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- 230000000712 assembly Effects 0.000 description 6
- 238000000429 assembly Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- JRMUNVKIHCOMHV-UHFFFAOYSA-M tetrabutylammonium bromide Chemical compound [Br-].CCCC[N+](CCCC)(CCCC)CCCC JRMUNVKIHCOMHV-UHFFFAOYSA-M 0.000 description 3
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 239000013256 coordination polymer Substances 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
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- 239000000706 filtrate Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- RCEAADKTGXTDOA-UHFFFAOYSA-N OS(O)(=O)=O.CCCCCCCCCCCC[Na] Chemical compound OS(O)(=O)=O.CCCCCCCCCCCC[Na] RCEAADKTGXTDOA-UHFFFAOYSA-N 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
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- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 1
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/01—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with flat filtering elements
- B01D29/03—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with flat filtering elements self-supporting
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a kind of decomposition of hydrate device, mixed gas separation system and separation method, the decomposition of hydrate device includes slurries separative unit and decomposition unit, and the slurries separative unit is connected to decomposition unit by interface channel；The slurries separative unit is divided into two parts up and down through filter screen separator component；The decomposition unit is disposed with the outlet of decomposition of hydrate gas, interface channel interface and regenerated liquid reservoir from top to bottom.Decomposer of the present invention can carry out efficient-decomposition to the hydrate slurry with mobility, and greatly reduce the energy consumption of reproduction operation liquid cooling reuse after hydrate slurry heating is decomposed and decomposed.The present invention also provides a kind of mixed gas separation system and method; material conveying is carried out by hydrate slurry form; cooperate decomposition of hydrate device of the invention, it is ensured that the good mobility of hydrate, it is ensured that separator continuity, scale, long-period stable operation.
Description
Technical field
The invention belongs to gas, liquid, solid phase separation fields, and in particular to a kind of decomposition of hydrate device and utilize Hydrate Technology
The system and method for separating gaseous mixture.
Background technique
Hydrate Technology is the hot spot of recent domestic research, in addition to as energy exploitation and application, gas hydrate phase
Pass technology has derived many new applications, for gas storage and transportation, gaseous mixture and solution separation, sewage treatment, sea water desalination,
CO2It seals up for safekeeping, the numerous areas such as Cool Storage Technology.2014, it was this that " the 8th international gas hydrates conference " is held in Beijing
Item conference is held in developing country for the first time, shows that China's hydrate research level has obtained world's approval, while will also be bound to
Cause the upsurge of domestic new round energy development and hydrate relation technological researching.In the application of numerous Hydrate Technologies, mixing
Gas isolation technics relies on the advantages that simple process, mild condition, flexible operation, green non-pollution largely to be paid close attention to.Hydrate
The principle of technology separation gaseous mixture is that the differing pressure of gas with various formation hydrate is very big, and gas with various is utilized to form hydrate
Pressure gap, by control formation condition, the separation of mixing gas component can be realized.Currently, hydrate separation technology quilt
Report is applied to grinding for the numerous areas gas purification such as natural gas, flue gas, coal bed gas, synthesis gas, refinery gas and biogas and purification
Study carefully.
The generating process of hydrate is similar to crystallization formation mechanism, including is nucleated and grows two processes, conventional aqueous object
The liquid phase that method separates gas uses aqueous solution, and the hydrate of generation is to be generally crystal habit, and hydrate can be at liquid-vapor interface
Agglomeration hinders vapor-liquid two phases contact, reduces hydration rate, and the hydrate mobility formed is poor, is easy aggregation blocking,
Directly constrain continuity, the scale application of hydrate the relevant technologies.But many researchs and patent be not to hydrate at present
Epidemic problem accounts for, such as patent CN1301684A, CN1272618A, CN101428190A, therefore also restricts it
The industrial applications of technology.For the flowability problem for solving hydrate, hydrate is processed by Mitsui shipbuilding Co., Ltd.
Spherical particle is conveyed, and needs to carry out dehydration procedure, recycles pelletizer to process dewatered hydrate, process is multiple
It is miscellaneous.Patent CN103030494A, CN101530719A, CN101554560A, CN1762929A etc. use hydrate slurry form,
The solution of hydrate and unreacted generation hydrate together circulation conveying is solved into flowability problem, but causes hydrate point
It needs integrally to heat up to mixed serum when solution, carries out whole cooling again after decomposing release gas, energy consumption has been significantly greatly increased, has improved
Operating cost.
Summary of the invention
For existing Separating Gas Mixtures via Hydrate Formation technology poor fluidity, the higher problem of decomposition of hydrate energy consumption, sheet
Invention provides a kind of decomposition of hydrate device, mixed gas separation system and separation method, it is ensured that the good mobility of hydrate,
While ensuring separator continuity, scale, long-period stable operation, greatly reduces and maintain hydrate mobility institute band
The problem of decomposition of hydrate and cooling energy consumption come increase.
In a first aspect, the present invention provides a kind of decomposition of hydrate device, the decomposition of hydrate device includes slurries separative unit
And decomposition unit, the slurries separative unit are connected to decomposition unit by interface channel；The slurries separative unit is through strainer
Baffle assembly is divided into two parts up and down, and top is disposed with hydrate slurry entrance, filter washing water inlet from top to bottom, connects and lead to
Pipeline joint, lower part are lonely liquid reservoir, and liquid storage trench bottom is equipped with cold purified liquor outlet；The decomposition unit is successively set from top to bottom
Be equipped with the outlet of decomposition of hydrate gas, interface channel interface and regenerated liquid reservoir, be provided in regenerated liquid reservoir heat exchange unit,
Stripping gas entrance, the outlet of regeneration hydrate working solution.
In above-mentioned decomposition of hydrate device, the interface channel is horizontally disposed or is obliquely installed at an angle, when
When being obliquely installed, slurries separative unit interface channel interface is made to be higher than decomposition unit interface channel interface, tilt angle and level
Face is at 10 °~60 °, preferably 15 °~45 °.The lower plane of interface channel is placed in the 1/2~3/4 of slurries separative unit vertical height
Place.
In above-mentioned decomposition of hydrate device, the filter screen separator component can be horizontally disposed with either to tilt at an angle and set
It sets, the upper plane of filter screen separator component and the lower plane of interface channel are arranged in same plane.The filter screen separator component uses
Any one of filling-material structure, screen net structure or mesh structure, realization are filtered processing to hydrate slurry, will be filtered
Rich hydrate phase slurries (or grain crystalline shape) are delivered to decomposition unit, and filtrate (lonely liquid) enters the reservoir of lower section.Strainer
The parameters such as aperture, porosity, the filling thickness of baffle assembly need for gaseous mixture system, additive types and form which kind of knot
Structure hydrate and be determined.
In above-mentioned decomposition of hydrate device, the hydrate slurry entrance is connected with spray assemblies, and the spray assemblies can be adopted
With liquid distribution trough well known in the art, it can be realized and hydrate slurry is sprayed and is uniformly distributed, guarantee that covering domain is entire
Slurries separative unit section.
In above-mentioned decomposition of hydrate device, the filter washing water inlet is connected with nozzle, and the nozzle can be used known in this field
Arbitrary form, can by cleaning solution high speed injection to filter screen separator component, area coverage accounts for entire filter screen separator component area
70% or more, realize that, to the washing souring of filter screen separator component, nozzle is arranged in certain inclination angle, inclined direction is towards company
Road is connected, tilt angle and median vertical line are at 5~45 °, and preferably 10~30 °.
In above-mentioned decomposition of hydrate device, the lonely liquid reservoir liquid holdup is the 1/3~2/3 of liquid storage sump volume.
In above-mentioned decomposition of hydrate device, the regenerated liquid reservoir liquid holdup is the 1/2~5/6 of liquid storage sump volume.
In above-mentioned decomposition of hydrate device, wall-type heat exchange equipment is provided in the heat exchange unit, it is logical that hot fluid walks tube side
It crosses coil form to heat hydrate slurry, fin can be added outside coil pipe for enhanced heat exchange.
In above-mentioned decomposition of hydrate device, multiple groups hydraulic barrier is set between the coil pipe of heat exchange equipment in the decomposition unit, is risen
To the effect of support coil pipe and enhanced heat transfer effect.
In above-mentioned decomposition of hydrate device, the stripping gas entrance is connected with gas distributor, and gas distributor and decomposition are single
The section of member is uniformly distributed in maximum, contacts stripping gas with rich hydrate slurry reverse flow in decomposition unit, the gas point
Gas distributor well known in the art can be used in cloth device, and the stripping gas can recycle for the regeneration gas of this unit decomposition, when again
When anger has subsequent rework process, stripping gas may be the arbitrary gas not reacted with following process process.
In above-mentioned decomposition of hydrate device, the regeneration hydrate working solution outlet of the decomposition unit bottom divides two-way, wherein
It is connect all the way through pipeline with the filter washing water inlet, the regeneration hydrate working solution that decomposed unit bottom is discharged is as in
Circulating cleaning fluid uses, and the regeneration hydrate working solution volume flow Zhan used as interior circulating cleaning fluid always regenerates hydration
The 1/5~1 of object working solution volume flow, preferably 1/3~1/2.
Second aspect, the present invention provide a kind of mixed gas separation system, and the separation system includes hydration reactor, hydration
Object decomposer and heat exchanger, the gaseous mixture feeding line are connect with hydrate reactor gas phase entrance, hydrate reactor
Liquid-phase outlet is connect through pipeline with the hydrate slurry entrance of decomposition of hydrate device slurries separative unit, the decomposition of hydrate device
Cold purified liquor outlet and regeneration hydrate working solution outlet connect after heat exchange equipment with the liquid phase entrance of hydrate reactor；Its
In, the decomposition of hydrate device includes slurries separative unit and decomposition unit, and the slurries separative unit and decomposition unit pass through
Interface channel connection；The slurries separative unit is divided into two parts up and down through filter screen separator component, and top is successively set from top to bottom
It is equipped with hydrate slurry entrance, filter washing water inlet, interface channel interface, lower part is lonely liquid reservoir, and liquid storage trench bottom is equipped with
Cold purified liquor outlet；The decomposition unit is disposed with the outlet of decomposition of hydrate gas, interface channel interface and regeneration from top to bottom
Liquid reservoir is provided with heat exchange unit, stripping gas entrance, the outlet of regeneration hydrate working solution in regenerated liquid reservoir.
In above-mentioned separation system, compressor is set on the gaseous mixture feeding line, for guaranteeing mixture pressure and water
Reactor operating pressure is closed to match.
In above-mentioned separation system, the decomposition of hydrate gas outlet is drawn a branch and is connect through pipeline with stripping gas entrance.
In above-mentioned separation system, the interface channel is horizontally disposed or is obliquely installed at an angle, works as inclination
When setting, make slurries separative unit interface channel interface be higher than decomposition unit interface channel interface, tilt angle and horizontal plane at
10 °~60 °, preferably 15 °~45 °.The lower plane of interface channel is placed at the 1/2~3/4 of slurries separative unit vertical height.
In above-mentioned separation system, the filter screen separator component level setting is either obliquely installed at an angle, strainer
The upper plane of baffle assembly will keep arranging with the lower plane of interface channel in same plane.The filter screen separator component is used and is filled out
Expect any one of structure, screen net structure or mesh structure, realization is filtered processing to hydrate slurry, by filtered richness
Hydrate phase slurries (or grain crystalline shape) are delivered to decomposition unit, and filtrate (lonely liquid) enters the reservoir of lower section.Strainer every
The parameters such as aperture, porosity, the filling thickness of board group part need for gaseous mixture system, additive types and form which kind of structure
Hydrate and be determined.
In above-mentioned separation system, the hydrate slurry entrance is connected with spray assemblies, this can be used in the spray assemblies
Liquid distribution trough well known to field, can be realized and hydrate slurry is sprayed and is uniformly distributed, and guarantee covering domain is entire slurries
Separative unit section.
In above-mentioned separation system, the filter washing water inlet is connected with nozzle, and the nozzle can be used well known in the art
Meaning form, can be by cleaning solution high speed injection to filter screen separator component, and area coverage accounts for the 70% of entire filter screen separator component area
More than, realize the washing souring to filter screen separator component, nozzle arranges that inclined direction is logical towards connection in certain inclination angle
Road, tilt angle and median vertical line are at 5~45 °, and preferably 10~30 °.
In above-mentioned separation system, the lonely liquid reservoir liquid holdup is the 1/3~2/3 of liquid storage sump volume.
In above-mentioned separation system, the regenerated liquid reservoir liquid holdup is the 1/2~5/6 of liquid storage sump volume.
In above-mentioned separation system, wall-type heat exchange equipment is provided in the heat exchange unit, hot fluid walks tube side and passes through disk
Form of tubes heats hydrate slurry, and fin can be added outside coil pipe for enhanced heat exchange.
In above-mentioned separation system, multiple groups hydraulic barrier is set between the coil pipe of heat exchange equipment in the decomposition unit, plays branch
The effect of support plate pipe and enhanced heat transfer effect.
In above-mentioned separation system, the stripping gas entrance is connected with gas distributor, gas distributor and decomposition unit
Section is uniformly distributed in maximum, contacts stripping gas with rich hydrate slurry reverse flow in decomposition unit, the gas distributor
Gas distributor well known in the art can be used, the stripping gas can recycle for the regeneration gas of this unit decomposition, work as regeneration gas
When having subsequent rework process, stripping gas may be the arbitrary gas not reacted with following process process.
In above-mentioned separation system, the regeneration hydrate working solution outlet of the decomposition unit bottom divides two-way, wherein all the way
It is connect through pipeline with the filter washing water inlet, the regeneration hydrate working solution that decomposed unit bottom is discharged is as interior circulation
Cleaning solution uses, and the regeneration hydrate working solution volume flow Zhan used as interior circulating cleaning fluid always regenerates hydrate work
Make the 1/5~1 of liquid volume flow, preferably 1/3~1/2.
In above-mentioned separation system, the hydration reactor for the benefit of gas-liquid mass transfer and with good heat transfer effect equipment,
Form is unlimited, can be one of stirring-type, atomizing, bubble type, sieve-board type, material filling type, hypergravity or shock flow type etc..
The third aspect, the present invention provide a kind of separation method of gaseous mixture, and the separation method includes the following steps:
(1) gaseous mixture enters hydration reactor, reacts with hydrate working solution, and the group of hydrate is easily generated in gaseous mixture
Divide and reacted with hydrate working solution, mutually form hydrate slurry into hydrate, is not easy to generate the component of hydrate in gas phase
Enrichment, and hydration reactor is discharged；
(2) hydrate slurry obtained in step (1) rich in gas enters decomposition of hydrate device, separates in the slurries of decomposer
After cell processing, lonely liquid and rich hydrate phase slurries are obtained, lonely liquid enters the lonely liquid reservoir of lower section；
(3) the rich hydrate phase slurries that step (2) obtains cleaned liquid effect, which enters in decomposition unit, to be handled, and with decomposition
Unit bottom is passed through stripping gas counter current contacting, and decomposition releases high concentration and is absorbed gas, and obtains regeneration hydrate working solution；
(4) lonely liquid obtained in step (2) mixes and the processing that cools down with regeneration hydrate working solution obtained in step (3)
Afterwards, hydration reactor is returned to be recycled.
In above-mentioned mixed gas separation method, the operating condition of the hydration reactor are as follows: pressure 0.1Mpa~5.0Mpa, temperature
0~15 DEG C of degree, concrete operations condition need to be determined for handled gaseous mixture system and the additive types of selection.
In above-mentioned mixed gas separation method, hydrate working solution described in step (1) can be aqueous solution, can also add
Various thermodynamics and kinetics promotors, such as lauryl sodium sulfate (SDS), sodium dodecylbenzenesulfonate (SDBS), linear alkane
Base sodium sulfonate (LAB-SA), alkyl polyglycoside (APG), tetrahydrofuran (THF), tetrabutylammonium bromide (TBAB), pentamethylene (CP) and
One or more of acetone.
In above-mentioned mixed gas separation method, hydrate working solution described in step (1) can also be oil mixing with water lotion, can
The preferable oily substance of mobility is added in working solution, such as one or more of kerosene, diesel oil and silicone oil, and is cooperated hydrophilic
Property emulsifier uses simultaneously.
In above-mentioned mixed gas separation method, in step (1) described hydration reactor, hydrate slurry, which refers to, has formed hydrate
The mixed solution of hydrate working solution is generated with unreacted, it is 30% that reaction controlling hydrate, which accounts for the volume ratio in hydrate slurry,
~80%, preferably 50%~70%.
In above-mentioned mixed gas separation method, the operating condition of step (2) the decomposition of hydrate device are as follows: pressure 0.05Mpa
~3.0Mpa, 0~10 DEG C of separative unit temperature, 10~40 DEG C of decomposition unit temperature.
In above-mentioned mixed gas separation method, hydrate slurry is divided into lonely liquid and rich water by step (2) slurries separative unit
Object phase slurries are closed, the hydrate volume content in lonely liquid is lower than 10%, and the hydrate volume content in rich hydrate phase slurries is high
In 80%.
In above-mentioned mixed gas separation method, step (2) described stripping gas, which can be, not to react with following process process
Arbitrary gas, such as nitrogen, inert gas is also possible to the decomposition gas part circulation that decomposition unit obtains.
In above-mentioned mixed gas separation method, hydrate is regenerated obtained in lonely liquid obtained in step (2) and step (3)
Working solution mixes and the hydration reactor temperature being cooled in step (1) matches, and returns to hydration reactor and is recycled.
In above-mentioned mixed gas separation method, the gaseous mixture can be the gaseous mixture purification (CH of natural gas and biogas4/
CO2), flue gas decarbonization (N2/CO2), coal bed gas separate (CH4/N2), synthesis gas decarbonization (CO2/H2), oil refinery dry gas recycling (lighter hydrocarbons/
H2) processing etc..
Heat in the decomposition of hydrate device of the method for the present invention can be heated using steam, also can use high-temperature flue gas or
Tail gas can also utilize the reaction heat and process waste heat of peripheral device.
Compared with prior art, decomposition of hydrate device of the present invention, mixed gas separation system and separation method have such as
Lower advantage:
(1) decomposition of hydrate device provided by the invention have slurries separative unit and decomposition unit, respectively to hydrate slurry into
Row is separated by filtration and deep decomposition.Hydrate slurry is divided into rich hydrate phase and lonely liquid phase: lonely liquid by slurries separative unit
Hemihydrate content in phase is extremely low, it is not necessary to heat up, can maintain lower temperature reuse；Hydrate in rich hydrate phase
Occupancy volume is higher than 80%, carries out heating and decomposition treatment in decomposition unit, while high efficient heat exchanging and stripping means having been cooperated to strengthen hydration
Object decomposes, and washing of the reproduction operation liquid extension for slurries separative unit filter screen separator component is washed away.Point of such mode
Efficient-decomposition can be carried out to the hydrate slurry with mobility by solving device, and decomposition of hydrate is high-efficient, have self-cleaning function,
It is easy to maintain, and greatly reduce the energy consumption of working solution cooling reuse after hydrate slurry heating is decomposed and decomposed.
(2) mixed gas separation system and method provided by the invention, operating condition is mild, can be at 0 DEG C or more to gaseous mixture
It is separated, and operating pressure is moderate, and has process short, easy to operate flexible, highly-safe, environment friendly and pollution-free etc. excellent
Point.The material conveying between hydrate reactor and decomposition of hydrate device is carried out by hydrate slurry form, so that hydrate
With good mobility, while cooperating decomposition of hydrate device of the invention, it is mixed not only to solve restriction Hydrate Technology separation
The continuity problem of gas is closed, and greatly reduces and maintains hydrate mobility bring energy penalty, reduces device operation
Cost, it is ensured that separator continuity, scale, long-period stable operation.
Detailed description of the invention
Fig. 1 is decomposition of hydrate device structural schematic diagram of the present invention.
Fig. 2 is mixed gas separation system schematic of the present invention.
Specific embodiment
It elaborates below in conjunction with drawings and examples to decomposition of hydrate device and mixed gas separation system of the invention,
But it is not intended to limit the present invention.
As shown in Figure 1, the decomposer includes slurries separative unit and divides the present invention provides a kind of decomposition of hydrate device
Unit, the slurries separative unit and decomposition unit is solved to be connected to by interface channel 12；The slurries separative unit through strainer every
Board group part 5 is divided into two parts up and down, and top is disposed with hydrate slurry entrance 1, filter washing water inlet 3, connection from top to bottom
Channel interface 19, lower part are lonely liquid reservoir 6, and liquid storage trench bottom is equipped with cold purified liquor outlet 13；The decomposition unit from upper and
Under be disposed with decomposition of hydrate gas outlet 11, interface channel interface 20 and regenerated liquid reservoir 7, the regenerated liquid reservoir
Heat exchange unit 10, stripping gas entrance 8, regeneration hydrate working solution outlet 14 are disposed in 7 from top to bottom.Described in wherein
Separative unit hydrate slurry entrance 1 is connected with spray assemblies 2；The interior circulating cleaning fluid entrance 3 is connected with Washing spray nozzle 4；
The deep decomposition unit stripping gas entrance 8 is connected with stripping gas distributor 9；Described 10 one end of heat exchange equipment is heating agent entrance
15, the other end is heating agent outlet 16；Multiple groups hydraulic barrier 17 is set between the coil pipe of heat exchange unit in the regenerated liquid reservoir 7.
The decomposition of hydrate device course of work of the present invention is as follows: hydrate slurry passes through decomposition of hydrate device hydrate slurry
Liquid entrance 1 introduces decomposer, is sprayed downwards by spray assemblies 2, and spray and lower hydrate slurry are by filter screen separator component 5
Hydrate slurry is divided into rich hydrate phase and lonely liquid phase by filtration treatment, and the Washing spray nozzle 4 of 5 top of filter screen separator component is logical
It crosses circulating cleaning fluid realization in constantly spraying to wash away the washing of filter screen separator component 5, filtered lonely liquid falls to lonely
Liquid reservoir 6, lonely liquid follow bad to hydrate reactor recycling, rich hydrate in the cold purified liquor outlet 13 of liquid storage trench bottom
Enter regenerated liquid reservoir 7 by interface channel 12, rich hydrate exchanges heat in regenerated liquid reservoir 7 with heat exchange equipment 10
And the channel of the formation of hydraulic barrier 17 is passed sequentially through, rich hydrate is constantly thermally decomposed during the falling process and is discharged gas,
Stripping gas is passed through by stripping gas entrance 8 in 7 bottom of regenerated liquid reservoir simultaneously, stripping gas uniformly divides through stripping gas distributor 9
With hydrate slurry counter current contacting after cloth, what decomposition of hydrate released high concentration is absorbed gas from the bottom to top, eventually by
11 discharge of decomposition of hydrate gas outlet, the regeneration hydrate working solution after decomposition pass through the recycled water of 7 bottom of regenerated liquid reservoir
14 discharge of object working solution outlet is closed, partial regeneration hydrate working solution 18 enters slurries separative unit pair as interior circulating cleaning solution
Filter screen separator component 5 is washed, and remaining reproduction operation liquid is delivered to hydrate reactor after cooling is handled.
As shown in Fig. 2, the present invention also provides a kind of mixed gas separation system, the separation system includes hydration reactor
24, decomposition of hydrate device 27 and heat exchanger 29, wherein decomposition of hydrate device is using decomposition of hydrate device described in Fig. 1；Mixing
Gas feeding line 21 is connect with 24 gas phase entrance of hydrate reactor, and compressor 22 is provided on feeding line 21；Hydrate is anti-
The liquid-phase outlet of device is answered to connect through pipeline 26 with the hydrate slurry entrance of decomposition of hydrate device 27, hydrate reactor gas phase goes out
Mouth is connected with exhaust pipe 25 is separated；The lonely liquid outlet line 28 and reproduction operation liquid outlet line of the decomposition of hydrate device
31 connect with 29 entrance of heat exchange equipment, and heat exchange equipment outlet is connect through pipeline 30 with the liquid phase entrance of hydrate reactor 24；Water
The entrance for closing object decomposer heat exchange unit carrys out line 33 with heating agent and connect, the outlet of decomposition of hydrate device heat exchange unit and heating agent loop line
34 connections；The decomposition of hydrate gas outlet is connect with disintegrating and regeneration gas pipeline 32, and disintegrating and regeneration gas pipeline 32 draws a branch
Pipeline 35 is connect with the stripping gas entrance of decomposition of hydrate device 27；The stripping gas entrance and stripping gas of the decomposition of hydrate device 27
Pipeline 36 connects.
It is as follows to provide the process that mixed gas separation system handles gaseous mixture using the present invention: gaseous mixture 21 is through compressing
Machine 22 enters hydration reactor 24 after being pressurized, and in hydration reactor 24, the gas component for easily generating hydrate enters hydration
Object phase (solid liquid phase) forms slurries, is not easy to generate the component of hydrate and is discharged in gas phase enrichment, and by exhaust pipe 25, real
The separation of existing gaseous mixture.The hydrate slurry that gas is rich in hydration reactor is introduced into decomposition of hydrate device 27 through pipeline 26,
Slurries are handled in the separative unit of decomposer first, obtain lonely liquid and rich hydrate phase slurries, and lonely liquid enters lower section
Lonely liquid reservoir, and be discharged by pipeline 28, rich hydrate phase slurries enter decomposition unit.In the rich hydrate of decomposition unit
Slurries are by heat treatment, and the stripping gas counter current contacting being passed through with decomposition unit bottom, stripping gas used are external stripping gas
The tap line 35 that pipeline 36 or regeneration gas are drawn provides, and hydrate slurry decomposition releases high concentration and is absorbed gas, simultaneously
Regeneration hydrate working solution is obtained, the gas released is discharged by disintegrating and regeneration gas pipeline 32, regenerates hydrate working solution 31
Enter heat exchange equipment 29 together with lonely liquid 28 after cooling down, returns to hydration reactor 24 and be recycled.
Embodiment 1
Decomposition of hydrate device provided by the invention is selected, separating treatment, coal seam are carried out to coal bed gas using process flow shown in Fig. 2
CH in gas4Volume content is 40% or so, remaining is N2And O2Equal gases.Coal bed gas 21 is pressurized to 0.4Mpa by compressor 22
Afterwards, carry out hydration reaction into hydrate reactor 24 and hydrate working solution, 24 condition of hydration reactor be pressure 0.4Mpa,
4 DEG C of temperature, hydrate working solution is the aqueous solution containing 6% THF and 300ppm SDS of molar concentration, and reaction controlling hydrate is raw
60% or so of hydrate slurry totality accumulated amount is accounted at amount, CH in the gas 25 of hydration reactor is discharged in gaseous mixture after processing4Contain
Amount is lower than 5%, meets safety dumping requirement (CH4Explosion limit is 5%~15%)；Hydrate slurry 26 is delivered to hydrate point
Device 27 is solved, 27 condition of decomposition of hydrate device is pressure 0.1Mpa, and hydrate slurry 26 is divided into slurries separative unit accounts for slurries
The rich hydrate phase of total amount 70% and 30% lonely liquid phase, wherein in lonely liquid hemihydrate content about 9% or so enter lonely liquid
Reservoir, hemihydrate content 82% or so enters regenerated liquid reservoir in rich hydrate, and regenerated liquid reservoir passes through heat exchange equipment dimension
25 DEG C of temperature are held, CH in the gas 32 discharged in decomposition of hydrate device4Content > 80%, decompose release gas 1/3 return to regeneration
Liquid liquid storage trench bottom is used as stripping gas 35, obtained high concentration CH4Gas may be used as fuel or be further processed into day
Right gas product.The risk of explosion that not only avoids oxygen-enriched coal bed gas discharge is handled by above-mentioned technique coal bed gas, and
Recycling has obtained high concentration CH4Gas.Entire treatment process is not only able to guarantee the good mobility of hydrate in device, and
Hydrate slurry is regenerated using double tower stagewise decomposer, greatly reduces energy consumption.
Comparative example 1
It is same as Example 1, the difference is that, decomposition of hydrate device reaches same treatment effect using conventional single column form
When fruit, rich water is decomposed into since hydrate slurry is first passed through separative unit by double tower stagewise decomposer used in Example 1
Object phase and lonely liquid phase are closed, then only to rich hydrate (hemihydrate content 82%) the Xiang Jinhang deep decomposition for accounting for overall slurries 70%
Processing, and using conventional decomposition tower in this comparative example, needing to generate in hydrate and unreacted the slurries of hydrate, (hydrate contains
Amount 60%) whole heating, decomposes the regenerated liquid obtained after release gas and carries out whole cooling again, energy consumption has been significantly greatly increased, has improved
Operating cost.Compared with Example 1, working solution cooling overall energy consumption after the hydrate slurry heating of this comparative example is decomposed and decomposed
Increase by 40% or more.
Embodiment 2
Decomposition of hydrate device provided by the invention is selected, separating treatment is carried out to biogas using process flow shown in Fig. 2, in biogas
CH4Volume content is 60% or so, remaining is with CO2Based on foreign gas.Biogas 21 is pressurized to by compressor 22
After 0.4Mpa, hydration reaction is carried out into hydrate reactor 24 and hydrate working solution, 24 condition of hydration reactor is pressure
3 DEG C of 3.0Mpa, temperature, hydrate working solution are the aqueous solution containing volume fraction 4% CP and molar fraction 0.3%TBAB, reaction
Control hydrate production quantity accounts for 65% or so of hydrate slurry totality accumulated amount, and hydration reactor is discharged in gaseous mixture after processing
CH in gas 254Content 90% or so；Hydrate slurry 26 is delivered to decomposition of hydrate device 27,27 condition of decomposition of hydrate device
For pressure 0.8Mpa, hydrate slurry 26 is divided into the rich hydrate phase and 26% for accounting for slurries total amount 74% in slurries separative unit
Lonely liquid phase, wherein hemihydrate content about 8% or so enters lonely liquid reservoir, hemihydrate content in rich hydrate in lonely liquid
84% or so enters regenerated liquid reservoir, and regenerated liquid reservoir maintains 22 DEG C of temperature by heat exchange equipment, releases in decomposition of hydrate device
CO in the gas 32 put2Content is higher than 80%, decomposes the 1/2 of release gas and returns to regenerated liquid liquid storage trench bottom as stripping gas 35
It uses, obtained high concentration CO2Gas recycling.Biogas is handled by above-mentioned technique, has respectively obtained high concentration CH4Gas
The CO of body and high concentration2Gas, while purification to biogas, also by CO2Gas trapping has not only obtained premium fuel, but also real
CO is showed2Emission reduction has both the energy and environmental benefit.This technical process not only solves the problems, such as hydrate poor fluidity, it is ensured that
Separator continuity, scale, long-period stable operation, and hydrate slurry is carried out using double tower stagewise decomposer
Regeneration, greatly reduces energy consumption, to reduce device operating cost.
Comparative example 2
It is same as Example 2, the difference is that, decomposition of hydrate device reaches same treatment effect using conventional single column form
When fruit, 74% is decomposed into since hydrate slurry is first passed through separative unit by double tower stagewise decomposer used in Example 1
Rich hydrate phase and 26% lonely liquid phase, deep decomposition processing is mutually only then carried out to the rich hydrate for accounting for overall slurries 74%,
And using conventional decomposition tower in this comparative example, it needs the slurries that hydrate and unreacted are generated to hydrate integrally to heat up, decomposes
The regenerated liquid obtained after release gas carries out whole cooling again, and energy consumption has been significantly greatly increased, has improved operating cost.With embodiment 1
It compares, working solution cooling overall energy consumption increases by 35% or so after the hydrate slurry heating of this comparative example is decomposed and decomposed.
Claims (33)
1. a kind of decomposition of hydrate device, the decomposition of hydrate device includes slurries separative unit and decomposition unit, the slurries point
It is connected to decomposition unit by interface channel from unit；The slurries separative unit is divided into two up and down through filter screen separator component
Point, top is disposed with hydrate slurry entrance, filter washing water inlet, interface channel interface from top to bottom, and lower part is lonely liquid
Reservoir, liquid storage trench bottom are equipped with cold purified liquor outlet；The decomposition unit is disposed with decomposition of hydrate gas from top to bottom and goes out
Mouthful, interface channel interface and regenerated liquid reservoir, be provided with heat exchange unit, stripping gas entrance, recycled water in regenerated liquid reservoir
Close the outlet of object working solution.
2. decomposition of hydrate device described in accordance with the claim 1, wherein the interface channel is horizontally disposed either in certain
Angle tilt setting makes slurries separative unit interface channel interface be higher than decomposition unit interface channel interface when being obliquely installed,
Tilt angle and horizontal plane are at 10 °~60 °, preferably 15 °~45 °.
3. decomposition of hydrate device described in accordance with the claim 1, wherein it is single that the lower plane of the interface channel is placed in slurries separation
At the 1/2~3/4 of first vertical height.
4. decomposition of hydrate device described in accordance with the claim 1, wherein the filter screen separator component level setting is either in one
Determine angle tilt setting, the upper plane of filter screen separator component and the lower plane of interface channel are arranged in same plane.
5. decomposition of hydrate device described in accordance with the claim 1, wherein the filter screen separator component uses filling-material structure, silk screen
Any one of structure or mesh structure.
6. decomposition of hydrate device described in accordance with the claim 1, wherein the lonely liquid reservoir liquid holdup is liquid storage sump volume
1/3~2/3.
7. decomposition of hydrate device described in accordance with the claim 1, wherein the regenerated liquid reservoir liquid holdup is liquid storage sump volume
1/2~5/6.
8. decomposition of hydrate device described in accordance with the claim 1, wherein be provided with wall-type heat exchange in the heat exchange unit and set
Standby, hot fluid is walked tube side and is heated by coil form to hydrate slurry.
9. decomposition of hydrate device according to claim 8, wherein be arranged between the coil pipe of heat exchange equipment in the decomposition unit
Multiple groups hydraulic barrier.
10. decomposition of hydrate device described in accordance with the claim 1, wherein the regeneration hydrate of the decomposition unit bottom works
Liquid outlet divides two-way, wherein connecting all the way through pipeline with the filter washing water inlet, the regeneration that decomposed unit bottom is discharged
Hydrate working solution is used as interior circulating cleaning fluid.
11. a kind of mixed gas separation system, the separation system includes hydration reactor, decomposition of hydrate device and heat exchanger, institute
It states gaseous mixture feeding line to connect with hydrate reactor gas phase entrance, the liquid-phase outlet of hydrate reactor is through pipeline and hydration
The hydrate slurry entrance of object decomposer slurries separative unit connects, the cold purified liquor outlet and recycled water of the decomposition of hydrate device
The outlet of object working solution is closed to connect after heat exchange equipment with the liquid phase entrance of hydrate reactor；Wherein, the decomposition of hydrate device
Including slurries separative unit and decomposition unit, the slurries separative unit is connected to decomposition unit by interface channel；The slurry
Liquid separative unit through filter screen separator component be divided into up and down two parts, top be disposed with from top to bottom hydrate slurry entrance,
Filter washing water inlet, interface channel interface, lower part are lonely liquid reservoir, and liquid storage trench bottom is equipped with cold purified liquor outlet；The decomposition
Unit is disposed with the outlet of decomposition of hydrate gas, interface channel interface and regenerated liquid reservoir, regenerated liquid liquid storage from top to bottom
Heat exchange unit, stripping gas entrance, the outlet of regeneration hydrate working solution are provided in slot.
12. separation system according to claim 11, wherein compressor is arranged on the gaseous mixture feeding line, is used for
Guarantee that mixture pressure matches with hydration reactor operating pressure.
13. separation system according to claim 11, wherein draw a branch through pipeline in the decomposition of hydrate gas outlet
It is connect with stripping gas entrance.
14. separation system according to claim 11, wherein it is either in certain angle that the interface channel, which is horizontally disposed,
Degree is obliquely installed, and when being obliquely installed, so that slurries separative unit interface channel interface is higher than decomposition unit interface channel interface, is inclined
Rake angle and horizontal plane are at 10 °~60 °, preferably 15 °~45 °.
15. separation system according to claim 11, wherein the lower plane of the interface channel is placed in slurries separative unit
At the 1/2~3/4 of vertical height.
16. separation system according to claim 11, wherein the filter screen separator component level setting is either in certain
Angle tilt setting, the upper plane of filter screen separator component will keep arranging with the lower plane of interface channel in same plane.
17. separation system according to claim 11, wherein the filter screen separator component uses filling-material structure, silk screen knot
Any one of structure or mesh structure.
18. separation system according to claim 11, wherein the lonely liquid reservoir liquid holdup is liquid storage sump volume
1/3~2/3.
19. separation system according to claim 11, wherein the regenerated liquid reservoir liquid holdup is liquid storage sump volume
1/2~5/6.
20. separation system according to claim 11, wherein wall-type heat exchange equipment is provided in the heat exchange unit,
Hot fluid is walked tube side and is heated by coil form to hydrate slurry.
21. separation system according to claim 20, wherein be arranged between the coil pipe of heat exchange equipment in the decomposition unit more
Group hydraulic barrier.
22. separation system according to claim 11, wherein the regeneration hydrate working solution of the decomposition unit bottom goes out
Mouth divides two-way, wherein connecting all the way through pipeline with the filter washing water inlet, the regeneration that decomposed unit bottom is discharged is hydrated
Object working solution is used as interior circulating cleaning fluid.
23. a kind of separation method of gaseous mixture, using separation system described in any claim in claim 11-22, institute
Separation method is stated to include the following steps:
(1) gaseous mixture enters hydration reactor, reacts with hydrate working solution, and the group of hydrate is easily generated in gaseous mixture
Divide and reacted with hydrate working solution, mutually form hydrate slurry into hydrate, is not easy to generate the component of hydrate in gas phase
Enrichment, and hydration reactor is discharged；
(2) hydrate slurry obtained in step (1) rich in gas enters decomposition of hydrate device, separates in the slurries of decomposer
After cell processing, lonely liquid and rich hydrate phase slurries are obtained, lonely liquid enters the lonely liquid reservoir of lower section；
(3) the rich hydrate phase slurries that step (2) obtains cleaned liquid effect, which enters in decomposition unit, to be handled, and with decomposition
Unit bottom is passed through stripping gas counter current contacting, and decomposition releases high concentration and is absorbed gas, and obtains regeneration hydrate working solution；
(4) lonely liquid obtained in step (2) mixes and the processing that cools down with regeneration hydrate working solution obtained in step (3)
Afterwards, hydration reactor is returned to be recycled.
24. according to the mixed gas separation method described in claim 23, wherein the operating condition of the hydration reactor are as follows: pressure
Power 0.1Mpa~5.0Mpa, 0~15 DEG C of temperature.
25. according to the mixed gas separation method described in claim 23, wherein hydrate working solution described in step (1) is water
Solution, or the various thermodynamics and kinetics promotors of addition.
26. according to the mixed gas separation method described in claim 23, wherein hydrate working solution described in rapid (1) is grease
Mixed emulsion, adds the preferable oily substance of mobility in working solution, and the oily substance is in kerosene, diesel oil and silicone oil
One or more, and cooperate hydrophilic emulsifier while using.
27. according to the mixed gas separation method described in claim 23, wherein in step (1) described hydration reactor, hydrate
Slurries refer to that having formed hydrate and unreacted generates the mixed solution of hydrate working solution, and reaction controlling hydrate accounts for hydrate slurry
Volume ratio in liquid is 30%~80%, preferably 50%~70%.
28. according to the mixed gas separation method described in claim 23, wherein the operation of step (2) the decomposition of hydrate device
Condition are as follows: pressure 0.05Mpa~3.0Mpa, 0~10 DEG C of slurries separative unit temperature, 10~40 DEG C of decomposition unit temperature.
29. according to the mixed gas separation method described in claim 23, wherein step (2) slurries separative unit is by hydrate slurry
Liquid is divided into lonely liquid and rich hydrate phase slurries, and the hydrate volume content in lonely liquid is lower than 10%, in rich hydrate phase slurries
Hydrate volume content be higher than 80%.
30. according to the mixed gas separation method described in claim 23, wherein step (2) described stripping gas is not add with subsequent
The arbitrary gas that work process reacts.
31. according to the mixed gas separation method described in claim 30, wherein step (2) stripping gas is nitrogen or inertia
Gas.
32. according to the mixed gas separation method described in claim 23, wherein step (2) described stripping gas is that decomposition unit obtains
The decomposition gas arrived.
33. according to the mixed gas separation method described in claim 23, wherein lonely liquid obtained in step (2) and step (3)
Obtained in regeneration hydrate working solution mix and the hydration reactor temperature being cooled in step (1) matches, return and be hydrated
Reactor cycles use.
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| CN113117503A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for separating mixed gas by energy-saving hydrate method |
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Effective date of registration: 20230927 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |