CN107551818A - Methanol purge gas pressure energy recovery system and method - Google Patents
Methanol purge gas pressure energy recovery system and method Download PDFInfo
- Publication number
- CN107551818A CN107551818A CN201710844259.8A CN201710844259A CN107551818A CN 107551818 A CN107551818 A CN 107551818A CN 201710844259 A CN201710844259 A CN 201710844259A CN 107551818 A CN107551818 A CN 107551818A
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- Prior art keywords
- expanding
- expanding machine
- machine unit
- pressure
- expansion
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 238000010926 purge Methods 0.000 title claims abstract description 34
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000007789 gas Substances 0.000 claims abstract description 104
- 230000008595 infiltration Effects 0.000 claims abstract description 27
- 238000001764 infiltration Methods 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 27
- 239000012528 membrane Substances 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims description 9
- 230000006837 decompression Effects 0.000 claims description 8
- 238000011143 downstream manufacturing Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims description 2
- 239000003546 flue gas Substances 0.000 claims description 2
- 239000002440 industrial waste Substances 0.000 claims description 2
- 239000013067 intermediate product Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 239000000047 product Substances 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000012466 permeate Substances 0.000 abstract description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- 238000005057 refrigeration Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A methanol purge gas pressure energy recovery system comprises a permeate gas outlet of a membrane separation device, a first cooler, a pressurizing end of an expander unit and a second cooler which are sequentially connected; and a tail gas outlet of the membrane separation device, the heater, an expansion end of the expander unit and the third cooler are connected in sequence. Above-mentioned methyl alcohol purge gas pressure can recovery system, utilize the expander unit through special design, high-pressure tail gas passes through the expansion end expansion and does work, the infiltration gas then improves pressure through the pressure boost end, the pressure energy that is about to high-pressure tail gas shifts the infiltration gas, guarantee that the infiltration gas sends the required pressure of low reaches, thereby can reduce membrane back pressure, this means the front and back pressure differential of membrane in the membrane separation device that has increased, improve the separation effect of hydrogen, still rationally carry out recycle to high-pressure tail gas's pressure energy, economic benefits has been improved. In addition, a methanol purge gas pressure energy recovery method based on the methanol purge gas pressure energy recovery system is also provided.
Description
Technical field
The present invention relates to the energy-conserving and emission-cutting technology field of petroleum chemical industry, more particularly to a kind of methanol purge gas pressure energy
Recovery system and method.
Background technology
Useful constituent therein (mainly hydrogen) is reclaimed through membrane separation device in methanol purge gas, gained infiltration pneumatic transmission returns
Methanol synthesis unit recycles, and delivers to conversion procedure after the adjusted valve decompression of gained tail gas or is used as fuel gas.By under
The influence of pressure is swum, pressure needs to maintain certain pressure value after film, it means that the front and rear pressure difference of film is less than normal, Hydrogen Separation effect
It is poor；The pressure of another aspect tail gas does not decline substantially, and the pressure of (such as conversion procedure) is relatively low downstream, between the two
Pressure drop is typically realized by valve, causes pressure loss of energy.
The content of the invention
In consideration of it, being necessary to provide, a kind of separating effect is preferable, rationally utilizes the methanol purge gas pressure of tail gas pressure energy
Can recovery system and method.
A kind of methanol purge gas pressure energy recovery system, including membrane separation device, the first cooler, expanding machine unit,
Two coolers, heater and the 3rd cooler；
The membrane separation device ooze vent outlet, first cooler, the expanding machine unit pressurized end and
Second cooler is sequentially connected；
The offgas outlet of the membrane separation device, the heater, the expanding end of the expanding machine unit and described
Three coolers are sequentially connected.
In one embodiment, the expanding machine unit is single-stage expansion or multiple expansion, when the expanding machine unit is
During single-stage expansion, the expanding machine unit only includes an expanding machine；It is described swollen when the expanding machine unit is multiple expansion
Swollen machine unit includes at least two expanding machines, and now, the pressurized end of all expanding machines of the expanding machine unit is arranged in series, institute
The expanding end for stating all expanding machines of expanding machine unit is arranged in parallel.
In one embodiment, first cooler be one or both of water cooler, air cooler and refrigeration machine with
On combination；Second cooler is combination more than one or both of water cooler, air cooler and refrigeration machine；Described
Three coolers are combination more than one or both of water cooler, air cooler and refrigeration machine.
In one embodiment, the thermal source of the heater is the low-quality used heat in factory.
A kind of methanol purge gas pressure energy recovery method, comprises the following steps：
Methanol purge gas is divided into infiltration gas and tail gas by membrane separation device；
The pressurized end that the infiltration gas is cooled to after 40 DEG C again by expanding machine unit is pressurized, the infiltration gas after supercharging
After being cooled to 40 DEG C, fed downstream process；
It is depressured after the tail gas heating by the expanding end expansion work of the expanding machine unit, the tail gas cooling after decompression
To after 40 DEG C, fed downstream process.
In one embodiment, the expanding machine unit is single-stage expansion or multiple expansion, when the expanding machine unit is
During single-stage expansion, the expanding machine unit only includes an expanding machine；It is described swollen when the expanding machine unit is multiple expansion
Swollen machine unit includes at least two expanding machines, and now, the pressurized end of all expanding machines of the expanding machine unit is arranged in series, institute
The pressurized end supercharging that infiltration gas passes sequentially through all expanding machines is stated, the expanding end of all expanding machines of the expanding machine unit is in parallel
Set, the tail gas is divided into and the expanding machine quantity identical tributary included by the expanding machine unit, difference expansion work drop
Converge after pressure.
In one embodiment, flowmeter metering is first passed through before the tail gas heating.
In one embodiment, the temperature after the tail gas heating is 120 DEG C~200 DEG C.
In one embodiment, the tail gas pressure of the expanding end outlet of the expansion cell is according to required for lower procedure
Pressure determines.
Above-mentioned methanol purge gas pressure energy recovery system, using specially designed expanding machine unit, high pressure exhaust gas passes through
Expanding end expansion work, infiltration gas then improve pressure by pressurized end, i.e., the pressure energy of high pressure exhaust gas are transferred into infiltration gas, protects
Pressure needed for card infiltration pneumatic transmission to downstream, so as to reduce pressure after film, it means that add film in membrane separation device
Front and rear pressure difference, improve the separating effect of hydrogen, so realize methanol volume increase purpose, in addition, also rationally to high pressure exhaust gas
Pressure energy is recycled, and improves economic benefit.
Brief description of the drawings
Fig. 1 is the structural representation of methanol purge gas pressure energy recovery system；
Fig. 2 is the structural representation that expanding machine unit is multiple expansion.
Embodiment
In order that the objects, technical solutions and advantages of the present invention become apparent from, below in conjunction with drawings and Examples, to this hair
It is bright to be further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, and do not have to
It is of the invention in limiting.
As shown in figure 1, the methanol purge gas pressure energy recovery system 100 of an embodiment, including membrane separation device 10,
One cooler 20, expanding machine unit 30, the second cooler 40, the cooler 60 of heater 50 and the 3rd.
Membrane separation device 10 to ooze vent outlet, the first cooler 10, the pressurized end 32 and second of expanding machine unit cold
But device 40 is sequentially connected.
The offgas outlet of membrane separation device 10, the cooler 60 of expanding end 34 and the 3rd of the expanding machine unit of heater 50 according to
Secondary connection.
Expanding machine unit 30 can be single-stage expansion or multiple expansion.As shown in figure 1, when expanding machine unit is single-stage expansion
When, expanding machine unit only includes an expanding machine.
When raw material forms change or special operation condition be present, the stream of infiltration gas and tail gas after the separation of membrane separation device 10
It is larger to measure deviation, it may occur however that expanding end and the unmatched problem of pressurized end flow.Now, expanding machine unit 30 can be multistage
Expansion, now, expanding machine unit 30 can include at least two expanding machines, now, all expanding machines of expanding machine unit 30
Pressurized end is arranged in series, and the expanding end of all expanding machines of expanding machine unit is arranged in parallel.For example, Fig. 2 is refer to, expanding machine list
Member is multiple expansion, including the first expanding machine 36 and the second expanding machine 38.The pressurized end 362 and second of first expanding machine 36 expands
The pressurized end 382 of machine 38 is arranged in series, and the expanding end 384 of the expanding machine 38 of expanding end 364 and second of the first expanding machine 36 is in parallel
Set.The He of pressurized end 362 of the first expanding machine 36 is passed sequentially through from the infiltration gas for oozing vent outlet outflow of membrane separation device 10
The pressurized end 382 of second expanding machine 38 is pressurized.The tail gas flowed out from the offgas outlet of membrane separation device 10 is divided into two strands, two strands of tails
After qi leel does not distinguish expansion work decompression by the expanding end 384 of the expanding machine 38 of expanding end 364 and second of the first expanding machine 36
Enter the 3rd cooler 50 after converging again.
It is appreciated that the first cooler 20 can be more than one or both of water cooler, air cooler and refrigeration machine
Combination.Second cooler 40 can be combination more than one or both of water cooler, air cooler and refrigeration machine.3rd cooling
Device 60 can be combination more than one or both of water cooler, air cooler and refrigeration machine., can basis in real work
It is actually needed and is selected.
The thermal source 50 of heater can be any quality waste heat in factory.Specifically, the thermal source 50 of heater can be
The production of low-pressure saturated steam, steam condensate, industrial waste gas, flue gas, the cooling water of exothermic reactor, temperature higher than normal temperature is given up
Liquid, the product for the processing that need to cool or intermediate products one or more therein.In real work, can according to be actually needed into
Row selection.Each mode of heating can be used in parallel, can also be used in series.
In addition, also providing the methanol purge gas pressure energy recovery method of an embodiment, the methanol purge gas pressure energy is returned
Receiving method is implemented based on above-mentioned methanol purge gas pressure energy recovery system 100, comprises the following steps：
S10, methanol purge gas are divided into infiltration gas and tail gas by membrane separation device.
The pressurized end that S20, infiltration gas are cooled to after 30~40 DEG C again by expanding machine unit is pressurized, the infiltration gas after supercharging
After being cooled to 30~40 DEG C, fed downstream process.
Specifically, in S20, infiltration gas is cooled to 30~40 DEG C by the first cooler 20 first, is passing through expanding machine list
The pressurized end supercharging of member 30, the infiltration gas after supercharging are cooled to 30~40 DEG C by the second cooler 40 again.
Specifically, expanding machine unit can be single-stage expansion or multiple expansion, it is swollen when expanding machine unit is single-stage expansion
Swollen machine unit only includes an expanding machine.When raw material forms change or special operation condition be present, after the separation of membrane separation device 10
Infiltration gas and tail gas flow deviation it is larger, it may occur however that expanding end and the unmatched problem of pressurized end flow.Now, expand
Machine unit can be multiple expansion, and now, expanding machine unit includes at least two expanding machines, and now, expanding machine unit owns
The pressurized end of expanding machine is arranged in series, and infiltration gas passes sequentially through the pressurized end supercharging of all expanding machines, and expanding machine unit owns
The expanding end of expanding machine is arranged in parallel, and tail gas is divided into and the expanding machine quantity identical tributary included by expanding machine unit, difference
Converge after expansion work decompression.
In S20, lower procedure is typically methanol-fueled CLC process.
It is depressured after S30, tail gas heating by the expanding end expansion work of expanding machine unit, the tail gas after decompression is cooled to 30
After~40 DEG C, fed downstream process.
Specifically, in S30, tail gas is dropped after being heated by heater 50 by the expanding end expansion work of expanding machine unit
Pressure, the tail gas after decompression are cooled to 40 DEG C through the 3rd cooler 60.
In one embodiment, flowmeter metering is first passed through before tail gas heating.
In one embodiment, the temperature after tail gas heating is 120 DEG C~200 DEG C.
Pressure of the tail gas pressure of the expanding end outlet of expanding machine unit according to required for lower procedure determines.Lower procedure
Can be methane conversion procedure or torch or the process used as fuel gas.
Above-mentioned methanol purge gas pressure energy recovery system 100, utilizes specially designed expanding machine unit 30, high pressure exhaust gas
By the expansion work of expanding end 34, infiltration gas then improves pressure by pressurized end 32, i.e., is transferred to the pressure energy of high pressure exhaust gas
Gas is permeated, ensures the pressure needed for infiltration pneumatic transmission to downstream, so as to reduce pressure after film, it means that add UF membrane
The front and rear pressure difference of film, improves the separating effect of hydrogen in device 10, and then realizes the purpose of methanol volume increase, in addition, also rationally right
The pressure energy of high pressure exhaust gas is recycled, and improves economic benefit.
Above-mentioned methanol purge gas pressure energy recovery method flow is simple, and improvement cost is low, and the cycle is short, at the same obtain energy-conservation and
Increase production two kinds of incomes, there is the characteristics of low input high yield.
Illustrated below so that Methanol Plant film carries hydrogen production device as an example, device charging is methanol purge gas, and pressure is about
5.1MPa, hydrogen therein is reclaimed using membrane separation process, influenceed by downstream unit, the pressure of pressure after film, i.e. infiltrating gas side
More than 2.6MPa is must be maintained at, therefore the front and rear pressure difference of film only has 3.5MPa.
On the one hand, because pressure difference is smaller, the rate of recovery of hydrogen is caused to only have 52%.On the other hand, membrane separation device is non-
The tail gas pressure of per-meate side maintains original pressure substantially, and the pressure of downstream unit need to maintain 2.6MPa, it is therefore desirable to uses
Regulating valve carries out reduced pressure treatment, causes pressure loss of energy.
Using above-mentioned methanol purge gas pressure energy recovery system 100, using special expansion cell, reclaimed by expanding end high
The pressure energy of tail gas is pressed, the pressure of infiltration gas is improved by pressurized end, after above-mentioned processing, pressure after film can be reduced, is improved
The front and rear pressure difference of film, so as to significantly improve hydrogen recovery rate, while the pressure energy of high pressure exhaust gas is also effectively reclaimed, had at one stroke
The effects obtained more.
Methanol purge gas pressure energy recovery method specific steps based on above-mentioned methanol purge gas pressure energy recovery system 100
It is as follows：
Pressurized end：It is about 1.4MPa to permeate atmospheric pressure, 40 DEG C is cooled to through the first cooler 20 first, then through pressurized end
2.6MPa is pressurized to, then is cooled to using the second cooler 40 after 40 DEG C and delivers to methanol-fueled CLC process.
Expanding end：High pressure exhaust gas pressure is about 6MPa, heater 50 is sent into after flowmeter measures, after being heated to 150 DEG C
Expanding end expansion work is delivered to, is depressurized to 2.6MPa, then delivers to conversion procedure after the 3rd cooler 60 is cooled to 40 DEG C.
Using above-mentioned methanol purge gas pressure energy recovery system 100 and method, the front and rear pressure difference of film brings up to 4.6MPa, hydrogen
Gas recovery rate is improved to 72.8%, significant effect.
Described above is only the preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
Member, under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be regarded as
Protection scope of the present invention.
Claims (7)
1. a kind of methanol purge gas pressure energy recovery system, it is characterised in that including membrane separation device, the first cooler, expansion
Machine unit, the second cooler, heater and the 3rd cooler；
The membrane separation device oozes vent outlet, first cooler, the pressurized end of the expanding machine unit and described
Second cooler is sequentially connected；
The offgas outlet of the membrane separation device, the heater, the expanding end of the expanding machine unit and described 3rd cold
But device is sequentially connected.
2. methanol purge gas pressure energy recovery system as claimed in claim 1, it is characterised in that the expanding machine unit is single
Level expansion or multiple expansion, when the expanding machine unit is single-stage expansion, the expanding machine unit only includes an expanding machine；
When the expanding machine unit is multiple expansion, the expanding machine unit includes at least two expanding machines, now, the expanding machine
The pressurized end of all expanding machines of unit is arranged in series, and the expanding end of all expanding machines of the expanding machine unit is arranged in parallel.
3. methanol purge gas pressure energy recovery system as claimed in claim 1, it is characterised in that the thermal source of the heater is
Any quality waste heat in factory, can be low-pressure saturated steam, steam condensate, industrial waste gas, flue gas, exothermic reactor
Cooling water, temperature are higher than production waste liquid, the product or intermediate products one or more therein of the processing that need to cool of normal temperature.
4. a kind of methanol purge gas pressure energy recovery method, it is characterised in that comprise the following steps：
Methanol purge gas is divided into infiltration gas and tail gas by membrane separation device；
The pressurized end that the infiltration gas is cooled to after 30~40 DEG C again by expanding machine unit is pressurized, the infiltration gas after supercharging
After being cooled to 30~40 DEG C, fed downstream process；
It is depressured after the tail gas heating by the expanding end expansion work of the expanding machine unit, the tail gas after decompression is cooled to 30
After~40 DEG C, fed downstream process.
5. methanol purge gas pressure energy recovery method as claimed in claim 4, it is characterised in that the expanding machine unit is single
Level expansion or multiple expansion, when the expanding machine unit is single-stage expansion, the expanding machine unit only includes an expanding machine；
When the expanding machine unit is multiple expansion, the expanding machine unit includes at least two expanding machines, now, the expanding machine
The pressurized end of all expanding machines of unit is arranged in series, and the infiltration gas passes sequentially through the pressurized end supercharging of all expanding machines, institute
The expanding end for stating all expanding machines of expanding machine unit is arranged in parallel, the tail gas be divided into the expanding machine unit included by
Expanding machine quantity identical tributary, converge respectively after expansion work decompression.
6. methanol purge gas pressure energy recovery method as claimed in claim 4, it is characterised in that the temperature after the tail gas heating
Spend for 120 DEG C~200 DEG C.
7. methanol purge gas pressure energy recovery method as claimed in claim 4, it is characterised in that the expansion of the expansion cell
Pressure of the tail gas pressure of mouth according to required for lower procedure is brought out to determine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710844259.8A CN107551818B (en) | 2017-09-18 | 2017-09-18 | Methanol purge gas pressure energy recovery system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710844259.8A CN107551818B (en) | 2017-09-18 | 2017-09-18 | Methanol purge gas pressure energy recovery system and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107551818A true CN107551818A (en) | 2018-01-09 |
| CN107551818B CN107551818B (en) | 2024-05-17 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN201710844259.8A Active CN107551818B (en) | 2017-09-18 | 2017-09-18 | Methanol purge gas pressure energy recovery system and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111362777A (en) * | 2020-04-21 | 2020-07-03 | 河北金牛旭阳化工有限公司 | Methanol synthesis system and methanol synthesis method |
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| CN101368221A (en) * | 2008-07-28 | 2009-02-18 | 洪国伟 | Dehumidification air feeding device for ironmaking blast furnace |
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