CN110440135A - A kind of VOCs recovery system based on LNG cold energy - Google Patents
A kind of VOCs recovery system based on LNG cold energy Download PDFInfo
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- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 267
- 238000011084 recovery Methods 0.000 title claims abstract description 42
- 238000001179 sorption measurement Methods 0.000 claims abstract description 81
- 238000004140 cleaning Methods 0.000 claims abstract description 33
- 238000009833 condensation Methods 0.000 claims abstract description 24
- 230000005494 condensation Effects 0.000 claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 24
- 238000010521 absorption reaction Methods 0.000 abstract description 7
- 239000007789 gas Substances 0.000 description 90
- 239000003949 liquefied natural gas Substances 0.000 description 74
- 238000002309 gasification Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 238000000746 purification Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 238000010792 warming Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 241001120493 Arene Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
Classifications
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- 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
- B01D53/002—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 by condensation
-
- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
- F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/14—Arrangements for supervising or controlling working operations for eliminating water
- F17D3/145—Arrangements for supervising or controlling working operations for eliminating water in gas pipelines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2221/00—Handled fluid, in particular type of fluid
- F17C2221/03—Mixtures
- F17C2221/032—Hydrocarbons
- F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The present invention provides a kind of VOCs recovery systems based on LNG cold energy, including LNG cold energy supply system, VOCs condensate recovery system and VOCs adsorption cleaning system, in LNG heat exchanger, cold energy is transferred in VOCs primary cooler and VOCs deep freezer by LNG using intermediate refrigerant, condensation liquefaction VOCs gas, and remaining VOCs gas is purified in adsorption tanks, the vapor in cold energy removing VOCs remaining in VOCs gas is then utilized in VOCs dehydrator.The present invention is using LNG as cold source, the utilization to LNG cold energy is realized by intermediate refrigerant, while improving LNG capacity usage ratio, LNG supply process is mutually separated with VOCs removal process, the regular supply for influencing LNG when VOCs condensate recovery system and adsorption cleaning system jam is effectively prevented, improves the safety of system, and compared with traditional VOCs absorption method, condensation method and absorption method are combined by the present invention, substantially increase the recovery efficiency of VOCs.
Description
Technical field
The present invention relates to VOCs recycling field more particularly to a kind of VOCs recovery systems based on LNG cold energy.
Background technique
Volatile organic matter (Volatile Organic Compounds, VOCs) is a series of volatile and inflammable has
The general name of the organic compound of poison is to cause the major reason of haze and PM2.5, and give birth to reduce heavily contaminated weather to people
It is endangered caused by work, the recycling and administration of VOCs need to be reinforced.
Domestic petroleum industry petroleum vapor recovery routine techniques mainly has absorption method, absorption process, membrane separation process, condensation method at present
Deng.Wherein, absorption method loss is big, operating cost is high；Absorption process equipment occupation space is big, operation energy consumption is high, and exhaust emissions is difficult to
Meet standard；Membrane separation process machine utilization is larger, and investment is high；Condensation method is limited by refrigerant, refrigerant and energy consumption, condensation temperature
Generally -40 DEG C~-70 DEG C, discharge standard cannot be not achieved completely by VOCs gas liquefaction.For solve refrigerating capacity it is insufficient,
LNG cold energy can be used for the condensing recovery of VOCs by the problem that the VOCs rate of recovery is low, exhaust emissions is not up to standard.
With increasingly strict and national positive implementation " coal changes gas " policy of environmental legislation, a large amount of liquefied natural gas
(liquefied natural gas, LNG) is used for the production of industry, LNG as -162 DEG C under normal pressure of super-low liquid,
Needing heating gasification before the use is NG, and the cold energy that LNG discharges during gasification is huge, about 840kJ/kg, this portion
Divide cold energy that there is considerable economic and social profit.
A kind of VOCs gas device using the recycling oil tank discharge of LNG cold energy that patent CN 206488547U is announced, will
LNG and VOCs gas are discharged into heat exchanger, directly utilize LNG cold energy condensation liquefaction VOCs gas, although this method realizes LNG
The utilization of cold energy, but due to after VOCs condensing recovery, without adsorption process, directly fixed gas being discharged into air, will lead to
VOCs discharge does not reach requirement, and since LNG and VOCs gas directly exchanges heat, as VOCs recovery system failure Shi Huiying
Ring the regular supply for arriving LNG.
Summary of the invention
In response to this problem, the present invention provides a kind of VOCs recovery system based on LNG cold energy, which utilizes intermediate refrigerant
LNG cold energy is used for the condensation liquefaction of VOCs by the utilization for realizing LNG cold energy, improves the capacity usage ratio of LNG, and is utilized
Remaining VOCs, improves the recovery efficiency of VOCs in adsorption tanks adsorption cleaning discharge gas.
Technical solution of the present invention:
A kind of VOCs recovery system based on LNG cold energy, including LNG cold energy supply system, VOCs condensate recovery system with
And VOCs adsorption cleaning system,
The LNG cold energy supply system is successively by LNG storage tank (1), LNG booster pump (2), LNG heat exchanger (3), air temperature gas
Change device (4), refrigerant circulation pump (5), VOCs deep freezer (6), VOCs primary cooler (7) composition, the outlet LNG storage tank (1) LNG warp
Pipeline is connect with LNG booster pump (2) entrance, and LNG booster pump (2) outlet connects through pipeline and LNG heat exchanger (3) tube-side inlet
It connects, LNG heat exchanger (3) the tube side outlet is connect through pipeline with air temperature gasifier (4) entrance, LNG heat exchanger (3) shell side
Outlet is connect through pipeline with refrigerant circulation pump (5) entrance, and refrigerant circulation pump (5) outlet is through pipeline and VOCs deep freezer (6)
Tube-side inlet connection, VOCs deep freezer (6) the tube side outlet is connect through pipeline with VOCs primary cooler (7) tube-side inlet, described
The outlet of VOCs primary cooler (7) tube side is connect through pipeline with LNG heat exchanger (3) shell side inlet, and wherein LNG heat exchanger (3) tube side is walked
LNG, shell side walk refrigerant；
The VOCs condensate recovery system is by VOCs deep freezer (6), VOCs primary cooler (7), booster fan (8), VOCs
It is dehydrator (9), first pipe separator (10), water collect tank (11), second pipe separator (12), gas-liquid separator (13), cold
Lime set storage tank (14) composition, booster fan (8) outlet is connect through pipeline with VOCs dehydrator (9) shell side inlet, described
VOCs dehydrator (9) shell-side outlet is connect through pipeline with first pipe separator (10) entrance, the first pipe separator
(10) leakage fluid dram is connect through pipeline with water collect tank (11) entrance, and first pipe separator (10) exhaust outlet is through pipeline and VOCs
The connection of primary cooler (7) shell side inlet, VOCs primary cooler (7) shell-side outlet is through pipeline and second pipe separator (12) entrance
Connection, second pipe separator (12) exhaust outlet are connect through pipeline with VOCs deep freezer (6) shell side inlet, second pipe
Connect after separator (12) drain line in road is in parallel with VOCs deep freezer (6) shell-side outlet pipeline with gas-liquid separator (13) entrance
It connects, gas-liquid separator (13) leakage fluid dram is connect through pipeline with condensate tank (14) entrance, and wherein VOCs deep freezer (6) is managed
Journey walks refrigerant, and shell side walks VOCs gas, and VOCs primary cooler (7) tube side walks refrigerant, and shell side walks VOCs gas；
The VOCs adsorption cleaning system is by VOCs dehydrator (9), gas-liquid separator (13), the first shut-off valve (15),
One adsorption tanks (16), the second shut-off valve (17), the second adsorption tanks (18) composition, the first shut-off valve (15) entrance pipe and the
It is connect after two shut-off valves (17) entrance pipe is in parallel with gas-liquid separator (13) exhaust outlet, the first shut-off valve (15) outlet warp
Pipeline is connect with the first adsorption tanks (16) entrance, and the second shut-off valve (17) outlet is through pipeline and the second adsorption tanks (18) entrance
Connection, after the first adsorption tanks (16) export pipeline is in parallel with the second adsorption tanks (18) export pipeline with VOCs dehydrator (9)
Tube-side inlet connection, VOCs dehydrator (9) the tube side outlet are connected with atmospheric environment, and wherein VOCs dehydrator (9) tube side is walked
Discharge gas after adsorption cleaning, shell side walk VOCs gas.
Refrigerant selects R22 in the LNG cold energy supply system.
The cryogenic temperature of the LNG heat exchanger (3) is -120~-140 DEG C, the cryogenic temperature of VOCs deep freezer (6) is -
100~-120 DEG C, the cryogenic temperature of VOCs primary cooler (7) is -60~-80 DEG C, the cryogenic temperature of VOCs dehydrator (9) is 0~-
10℃。
First adsorption tanks (16) are used alternatingly with the second adsorption tanks (18), when the first adsorption tanks (16) in use,
One shut-off valve (15) is opened, and the second shut-off valve (17) is closed, remaining in the first adsorption tanks (16) adsorption cleaning discharge gas
VOCs, when the first adsorption tanks (16) saturation, the second adsorption tanks (18) begin to use, and the second shut-off valve (17) is opened at this time, the
One shut-off valve (15) is closed, remaining VOCs in the second adsorption tanks (18) adsorption cleaning discharge gas.
The invention has the advantages that
1. -162 DEG C of use of LNG of the present invention is as cold source, real using intermediate refrigerant as the medium of transmitting LNG cold energy
The utilization of existing LNG cold energy can effectively prevent VOCs condensate recovery system and adsorption cleaning system compared with directly utilizing LNG cold energy
System influences the regular supply of LNG when breaking down, improve the safety of LNG supply.
2. not needing compressor operating in condensation process of the present invention, greatly reduces equipment investment cost and electricity consumption is negative
Lotus.
3. condensation method and absorption method are combined by the present invention, the rate of recovery of VOCs is improved, the row of VOCs is substantially reduced
High-volume.
Detailed description of the invention
Fig. 1 is the flow chart of the VOCs recovery system.
In figure: 1, LNG storage tank 2, LNG booster pump 3, LNG heat exchanger 4, air temperature gasifier
5, refrigerant circulation pumps 6, VOCs deep freezer 7, VOCs primary cooler 8, booster fan
9, VOCs dehydrator 10, first pipe separator 11, water collect tank 12, second pipe separator
13, gas-liquid separator 14, condensate tank 15, the first shut-off valve 16, the first adsorption tanks
17, the second shut-off valve 18, the second adsorption tanks
Specific embodiment
The present invention is described in further detail with reference to the accompanying drawing and by embodiment, and following embodiment is to this hair
Bright explanation and the invention is not limited to following embodiments.
Embodiment 1
As shown in Figure 1, a kind of VOCs recovery system based on LNG cold energy, including LNG cold energy supply system, VOCs condensation
Recovery system and VOCs adsorption cleaning system,
It is 50g/m from production link VOCs gas concentration in this example3, temperature is 40 DEG C, and type is mixing fragrance
Hydrocarbon.
In LNG cold energy supply system, the LNG come out from LNG storage tank (1) is after the pressurization of LNG booster pump (2), in LNG
Gasification is NG in heat exchanger (3), cold energy is passed to the R22 in VOCs condensate recovery system, NG temperature rises to -130 DEG C, then
NG is warming up to 25 DEG C in air temperature gasifier (4).R22 pumps (5) after LNG heat exchanger (3) is cooled to -120 DEG C, through refrigerant circulation
After pressurization, sequentially enters and discharge cold energy in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas, then
R22 is returned in LNG heat exchanger (3) and is condensed again, completes one cycle, is reached for the mesh of VOCs gas condensation supply cold energy
, wherein -115 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -70 DEG C.
In VOCs condensate recovery system, VOCs gas is after the pressurization of booster fan (8), VOCs condensate recovery system
In, into being cooled to -5 DEG C in VOCs dehydrator (9), vapor therein is deviate from condensation, prevents the vapor in VOCs gas
It freezes in follow-up process and causes channel blockage, influence system operation, and by condensed moisture in first pipe separator (10)
From and be discharged into water collect tank (11), it is dry after VOCs gas enter in VOCs primary cooler (7) through pipeline and be cooled to -60 DEG C, In
Condensate liquid is separated in second pipe separator (12), is cooled to -100 DEG C in VOCs deep freezer (6), is made the concentration of VOCs gas
It is reduced to 70mg/m3Afterwards, VOCs primary cooler (7) converges with the condensate liquid in VOCs deep freezer (6), into gas-liquid separator (13)
In, condensate liquid therein is separated with remnants VOCs gas, condensate liquid is delivered to condensate tank (14) storage, remaining VOCs gas
Body is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, remaining VOCs gas through the first shut-off valve (15) and the second shut-off valve (17),
Into utilizing the active carbon purifying in tank to 4mg/m in the first adsorption tanks (16) and the second adsorption tanks (18)3, gas temperature after purification
Degree rises to -16 DEG C, subsequently into VOCs dehydrator (9), is removed VOCs gas cooling to -5 DEG C using its remaining cold energy
Vapor in VOCs gas, is finally discharged into atmosphere for purified gas, wherein the first adsorption tanks (16) and the second adsorption tanks
(18) it is used alternatingly, when the first adsorption tanks (16) in use, the first shut-off valve (15) is opened, the second shut-off valve (17) is closed, the
Remaining VOCs in one adsorption tanks (16) adsorption cleaning discharge gas, when the first adsorption tanks (16) saturation, the second adsorption tanks
(18) begin to use, the second shut-off valve (17) is opened at this time, and the first shut-off valve (15) is closed, the second adsorption tanks (18) adsorption cleaning
Remaining VOCs in discharge gas.
Embodiment 2
In this example, consistent from production link VOCs gas temperature and type and embodiment 1, concentration rises to 100g/
m3。
In LNG cold energy supply system, LNG gasification in LNG heat exchanger (3) is NG, and cold energy is passed to VOCs condensation
R22 in recovery system, NG temperature rise to -129 DEG C, and then NG is warming up to 25 DEG C in air temperature gasifier (4).R22 is changed in LNG
After hot device (3) is cooled to -120 DEG C, sequentially enter in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas
Body, wherein -113 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -68 DEG C.
In VOCs condensate recovery system, VOCs gas is cooled to -5 DEG C in VOCs dehydrator (9), removes VOCs gas
In vapor condensed water is discharged into water collect tank (11) and in first pipe separator (10), it is dry after VOCs gas exist
VOCs primary cooler is cooled to -60 DEG C in (7), condensate liquid is separated in second pipe separator (12), in VOCs deep freezer (6)
- 100 DEG C are cooled to, the concentration of VOCs gas is made to be reduced to 71mg/m3Afterwards, condensate liquid converges, and divides into pipeline to gas-liquid
From in device (13), VOCs condensate liquid is discharged into storage tank (14), remaining VOCs gas is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, the adsorption cleaning process and reality of the first adsorption tanks (16) and the second adsorption tanks (18)
It is consistent to apply example 1, but since VOCs concentration increases, the VOCs concentration after purification in discharge gas rises to 5mg/m3, temperature rises to -15
DEG C, wherein remaining cold energy by VOCs gas cooling to -5 DEG C, removes in VOCs gas in VOCs dehydrator (9) for utilization
Purified discharge gas is finally discharged into air by vapor.
Embodiment 3
In this example, consistent from production link VOCs gas temperature and type and embodiment 1, concentration rises to 150g/
m3。
In LNG cold energy supply system, LNG gasification in LNG heat exchanger (3) is NG, and cold energy is passed to VOCs condensation
R22 in recovery system, NG temperature rise to -128 DEG C, and then NG is warming up to 25 DEG C in air temperature gasifier (4).R22 is changed in LNG
After hot device (3) is cooled to -120 DEG C, sequentially enter in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas
Body, wherein -110 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -65 DEG C.
In VOCs condensate recovery system, VOCs gas is cooled to -5 DEG C in VOCs dehydrator (9), removes VOCs gas
In vapor condensed water is discharged into water collect tank (11) and in first pipe separator (10), it is dry after VOCs gas exist
VOCs primary cooler is cooled to -60 DEG C in (7), condensate liquid is separated in second pipe separator (12), in VOCs deep freezer (6)
- 100 DEG C are cooled to, the concentration of VOCs gas is made to be reduced to 72mg/m3Afterwards, condensate liquid converges, and divides into pipeline to gas-liquid
From in device (13), VOCs condensate liquid is discharged into storage tank (14), remaining VOCs gas is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, the adsorption cleaning process and reality of the first adsorption tanks (16) and the second adsorption tanks (18)
It is consistent to apply example 1, but since VOCs concentration increases, the VOCs concentration after purification in discharge gas rises to 6mg/m3, temperature rises to -13
DEG C, wherein remaining cold energy by VOCs gas cooling to -5 DEG C, removes in VOCs gas in VOCs dehydrator (9) for utilization
Purified discharge gas is finally discharged into air by vapor.
Embodiment 4
It in this example, is 50g/m from production link VOCs gas concentration3, temperature is 40 DEG C, and VOCs type is gasoline
Oil gas.
In LNG cold energy supply system, LNG gasification in LNG heat exchanger (3) is NG, and cold energy is passed to VOCs condensation
R22 in recovery system, NG temperature rise to -136 DEG C, and then NG is warming up to 25 DEG C in air temperature gasifier (4).R22 is changed in LNG
After hot device (3) is cooled to -120 DEG C, sequentially enter in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas
Body, wherein -120 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -76 DEG C.
In VOCs condensate recovery system, VOCs gas is cooled to -5 DEG C in VOCs dehydrator (9), removes VOCs gas
In vapor condensed water is discharged into water collect tank (11) and in first pipe separator (10), it is dry after VOCs gas exist
VOCs primary cooler is cooled to -60 DEG C in (7), condensate liquid is separated in second pipe separator (12), in VOCs deep freezer (6)
- 100 DEG C are cooled to, the concentration of VOCs gas is made to be reduced to 90mg/m3Afterwards, condensate liquid converges, and divides into pipeline to gas-liquid
From in device (13), VOCs condensate liquid is discharged into storage tank (14), remaining VOCs gas is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, the adsorption cleaning process and reality of the first adsorption tanks (16) and the second adsorption tanks (18)
It is consistent to apply example 1, the VOCs concentration after purification in discharge gas is down to 30mg/m3, temperature rises to -20 DEG C, and utilization is wherein remaining
Cold energy is in VOCs dehydrator (9), by VOCs gas cooling to -5 DEG C, removes the vapor in VOCs gas, finally will purification
Discharge gas afterwards is discharged into air.
Embodiment 5
In this example, the VOCs gas temperature from production link and type and embodiment 4 are consistent, and concentration rises to
100g/m3。
In LNG cold energy supply system, LNG gasification in LNG heat exchanger (3) is NG, and cold energy is passed to VOCs condensation
R22 in recovery system, NG temperature rise to -135 DEG C, and then NG is warming up to 25 DEG C in air temperature gasifier (4).R22 is changed in LNG
After hot device (3) is cooled to -120 DEG C, sequentially enter in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas
Body, wherein -118 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -74 DEG C.
In VOCs condensate recovery system, VOCs gas is cooled to -5 DEG C in VOCs dehydrator (9), removes VOCs gas
In vapor condensed water is discharged into water collect tank (11) and in first pipe separator (10), it is dry after VOCs gas exist
VOCs primary cooler is cooled to -60 DEG C in (7), condensate liquid is separated in second pipe separator (12), in VOCs deep freezer (6)
- 100 DEG C are cooled to, the concentration of VOCs gas is made to be reduced to 91mg/m3Afterwards, condensate liquid converges, and divides into pipeline to gas-liquid
From in device (13), VOCs condensate liquid is discharged into storage tank (14), remaining VOCs gas is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, the adsorption cleaning process and reality of the first adsorption tanks (16) and the second adsorption tanks (18)
It is consistent to apply example 1, but since VOCs concentration increases, the VOCs concentration after purification in discharge gas rises to 31mg/m3, temperature rises to-
18 DEG C, wherein remaining cold energy by VOCs gas cooling to -5 DEG C, removes in VOCs gas in VOCs dehydrator (9) for utilization
Vapor, finally purified discharge gas is discharged into air.
Embodiment 6
In this example, the VOCs gas temperature from production link and type and embodiment 4 are consistent, and concentration rises to
150g/m3。
In LNG cold energy supply system, LNG gasification in LNG heat exchanger (3) is NG, and cold energy is passed to VOCs condensation
R22 in recovery system, NG temperature rise to -134 DEG C, and then NG is warming up to 25 DEG C in air temperature gasifier (4).R22 is changed in LNG
After hot device (3) is cooled to -120 DEG C, sequentially enter in VOCs deep freezer (6) and VOCs primary cooler (7), condensation liquefaction VOCs gas
Body, wherein -116 DEG C are risen in VOCs deep freezer (6) exit R22 temperature, in VOCs primary cooler (7) exit R22 temperature liter
To -71 DEG C.
In VOCs condensate recovery system, VOCs gas is cooled to -5 DEG C in VOCs dehydrator (9), removes VOCs gas
In vapor condensed water is discharged into water collect tank (11) and in first pipe separator (10), it is dry after VOCs gas exist
VOCs primary cooler is cooled to -60 DEG C in (7), condensate liquid is separated in second pipe separator (12), in VOCs deep freezer (6)
- 100 DEG C are cooled to, the concentration of VOCs gas is made to be reduced to 92mg/m3Afterwards, condensate liquid converges, and divides into pipeline to gas-liquid
From in device (13), VOCs condensate liquid is discharged into storage tank (14), remaining VOCs gas is discharged into VOCs adsorption cleaning system.
In VOCs adsorption cleaning system, the adsorption cleaning process and reality of the first adsorption tanks (16) and the second adsorption tanks (18)
It is consistent to apply example 1, but since VOCs concentration increases, the VOCs concentration after purification in discharge gas rises to 32mg/m3, temperature rises to-
15 DEG C, wherein remaining cold energy by VOCs gas cooling to -5 DEG C, removes in VOCs gas in VOCs dehydrator (9) for utilization
Vapor, finally purified discharge gas is discharged into air.
In conclusion the present invention handles the VOCs gas of variety classes, concentration, the VOCs of discharge gas after processing
Concentration is below 80mg/m3Provincial standard and 120mg/Nm3National standard, recovery efficiency is above 99.9%, especially right
It is more preferable in mixed arenes gas purifying effect.
Claims (4)
1. a kind of VOCs recovery system based on LNG cold energy characterized by comprising LNG cold energy supply system, VOCs condensation
Recovery system and VOCs adsorption cleaning system,
The LNG cold energy supply system is successively by LNG storage tank (1), LNG booster pump (2), LNG heat exchanger (3), air temperature gasifier
(4), refrigerant circulation pump (5), VOCs deep freezer (6), VOCs primary cooler (7) composition, the outlet LNG storage tank (1) LNG is through pipeline
It being connect with LNG booster pump (2) entrance, LNG booster pump (2) outlet is connect through pipeline with LNG heat exchanger (3) tube-side inlet,
LNG heat exchanger (3) the tube side outlet is connect through pipeline with air temperature gasifier (4) entrance, and LNG heat exchanger (3) shell side goes out
Mouth is connect through pipeline with refrigerant circulation pump (5) entrance, and refrigerant circulation pump (5) outlet is through pipeline and VOCs deep freezer (6) pipe
The connection of journey entrance, VOCs deep freezer (6) the tube side outlet is connect through pipeline with VOCs primary cooler (7) tube-side inlet, described
The outlet of VOCs primary cooler (7) tube side is connect through pipeline with LNG heat exchanger (3) shell side inlet, and wherein LNG heat exchanger (3) tube side is walked
LNG, shell side walk refrigerant；
The VOCs condensate recovery system is dehydrated by VOCs deep freezer (6), VOCs primary cooler (7), booster fan (8), VOCs
Device (9), first pipe separator (10), water collect tank (11), second pipe separator (12), gas-liquid separator (13), condensate liquid
Storage tank (14) composition, booster fan (8) outlet are connect through pipeline with VOCs dehydrator (9) shell side inlet, the VOCs
Dehydrator (9) shell-side outlet is connect through pipeline with first pipe separator (10) entrance, first pipe separator (10) row
Liquid mouth is connect through pipeline with water collect tank (11) entrance, and first pipe separator (10) exhaust outlet is through pipeline and VOCs primary cooler
(7) shell side inlet connects, and VOCs primary cooler (7) shell-side outlet is connect through pipeline with second pipe separator (12) entrance,
Second pipe separator (12) exhaust outlet is connect through pipeline with VOCs deep freezer (6) shell side inlet, the second pipe point
It is connect after in parallel with VOCs deep freezer (6) shell-side outlet pipeline from device (12) drain line with gas-liquid separator (13) entrance, institute
It states gas-liquid separator (13) leakage fluid dram and is connect through pipeline with condensate tank (14) entrance, wherein VOCs deep freezer (6) tube side is walked
Refrigerant, shell side walk VOCs gas, and VOCs primary cooler (7) tube side walks refrigerant, and shell side walks VOCs gas；
The VOCs adsorption cleaning system is inhaled by VOCs dehydrator (9), gas-liquid separator (13), the first shut-off valve (15), first
Attached tank (16), the second shut-off valve (17), the second adsorption tanks (18) composition, the first shut-off valve (15) entrance pipe and second section
It is connect after only valve (17) entrance pipe is in parallel with gas-liquid separator (13) exhaust outlet, the first shut-off valve (15) outlet is through pipeline
It is connect with the first adsorption tanks (16) entrance, the second shut-off valve (17) outlet connects through pipeline and the second adsorption tanks (18) entrance
It connects, is managed after the first adsorption tanks (16) export pipeline is in parallel with the second adsorption tanks (18) export pipeline with VOCs dehydrator (9)
The connection of journey entrance, VOCs dehydrator (9) the tube side outlet are connected with atmospheric environment, and wherein VOCs dehydrator (9) tube side is walked to inhale
Attached purified discharge gas, shell side walk VOCs gas.
2. a kind of VOCs recovery system based on LNG cold energy according to claim 1, it is characterised in that: the LNG cold energy
Refrigerant selects R22 in supply system.
3. a kind of VOCs recovery system based on LNG cold energy according to claim 1, it is characterised in that: the LNG heat exchange
The cryogenic temperature of device (3) is -120~-140 DEG C, and the cryogenic temperature of VOCs deep freezer (6) is -100~-120 DEG C, cold at the beginning of VOCs
The cryogenic temperature of device (7) is -60~-80 DEG C, and the cryogenic temperature of VOCs dehydrator (9) is 0~-10 DEG C.
4. a kind of VOCs recovery system based on LNG cold energy according to claim 1, it is characterised in that: described first inhales
Attached tank (16) is used alternatingly with the second adsorption tanks (18), when the first adsorption tanks (16) in use, the first shut-off valve (15) is opened, the
Two shut-off valves (17) are closed, remaining VOCs in the first adsorption tanks (16) adsorption cleaning discharge gas, when the first adsorption tanks (16)
When saturation, the second adsorption tanks (18) begin to use, and the second shut-off valve (17) is opened at this time, and the first shut-off valve (15) is closed, and second
Remaining VOCs in adsorption tanks (18) adsorption cleaning discharge gas.
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