CN107460015A - A kind of deep natural gas dewatering system device and dewatering - Google Patents
A kind of deep natural gas dewatering system device and dewatering Download PDFInfo
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- CN107460015A CN107460015A CN201710904837.2A CN201710904837A CN107460015A CN 107460015 A CN107460015 A CN 107460015A CN 201710904837 A CN201710904837 A CN 201710904837A CN 107460015 A CN107460015 A CN 107460015A
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- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/1431—Pretreatment by other processes
- B01D53/145—Pretreatment by separation of solid or liquid material
-
- 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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/24—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 centrifugal force
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a kind of deep natural gas dewatering system device, it is characterised in that：Including filter separator, the first hypergravity machine, condenser, lean/rich liquid heat exchanger, booster pump, surge tank, reboiler, the second hypergravity machine, flash tank, delivery pump, the first stop valve, the second stop valve, the 3rd stop valve, the 4th stop valve, the 5th stop valve, pressure-reducing valve, flowmeter, vavuum pump, gas-liquid separator and triple valve；The invention also discloses a kind of dewatering；The purity of triethylene glycol lean solution after regeneration can be brought up to 99.99wt% by apparatus of the present invention, absorbent is used as using the triethylene glycol lean solution, the gas outlet water dew point through water suction processing in absorption system can be made to be reduced to less than 35 DEG C, preferably can be to being down to less than 45 DEG C；Solves the dewater treatment requirement for because of the low problem of gas dehydration depth in absorption system caused by triethylene glycol purity is not high, meeting low water dew point natural gas.
Description
Technical field
The present invention relates to petroleum gas processing technical field, more particularly, to a kind of deep natural gas dewatering system
Device and dewatering.
Background technology
Natural gas is a kind of fuel of cleaning, and Air-pollution From Combustion is small, calorific value is high, and shared status is got in modern energy structure
Come more important.But natural gas all contains substantial amounts of vapor when being produced from oil gas field or after desulfurization process, is deposited in natural gas
Water some problem can be produced in the processing of natural gas and transmitting procedure.Saturated steam in natural gas can be specific
Condensed under temperature and pressure and form solid hydrate, and the environment of cryogenic high pressure can aggravate this phenomenon, solid-state it is crystalline
Hydrate can cause the blockage problem of pipeline, instrument and valve, and the safe transport to natural gas brings potential danger.In addition, day
Sour gas, such as hydrogen sulfide and carbon dioxide also be present in right gas, these sour gas and moisture combination can form acid
Matter, transfer pipeline and equipment are caused to corrode.
At present, the method for conventional gas dehydration has solid absorption method, solvent absorption, freezing separation method etc..This three
The dehydration depth highest of solid absorption method in kind method, but its infrastructure investment is high, adsorbent reactivation high energy consumption, therefore it is applied
Scope is restricted.Solvent absorption is because simple to operate, and treating capacity is method preferred in current commercial Application greatly, this method
In widely used triethylene glycol as absorbent.TEG dehydration system is by Gas Dehydration System and triethylene glycol regenerative system two
It is grouped into.Traditional triethylene glycol dehydration mainly using packed tower as dehydration device, rectifying column as regenerating unit, there is with
Lower shortcoming：1st, tower size is big, and mass-transfer efficiency is low, and investment is higher, difficult into sled；2nd, triethylene glycol regeneration temperature is high, system energy consumption
It is larger.
High-gravity technology is a kind of process intensification emerging technology that can strengthen mass transfer.High-gravity technology is using at a high speed
Centrifugal force caused by the rotor of rotation, liquid is ground into extremely small liquid film, drop, boundary renewal speed is accelerated, greatly
It is big to strengthen mass transport process, there is the advantages of short residence time, simple to operate, vapour-liquid mass efficiency high, equipment size is small.
Chinese invention patent CN201410490633 report a kind of gravity Method triethylene glycol Gas Dehydration System and its
Technique, this technique, as absorption and regenerating unit, improve triethylene glycol-gas dehydration body using cross_flow rotating packed bed
The mass-transfer efficiency of system, simplifies Gas Dehydration System, reduces the size of dehydration equipment.This system and technique are minimum can be with
Triethylene glycol lean solution is regenerated to 99.0% purity, gas dehydration, aqueous dew point temperature are carried out using the triethylene glycol. solution of the purity
It is minimum to be down to about -18 DEG C, the requirement of natural gas transportation at a temperature of general environment is can reach, is met in some techniques at the beginning of natural gas
Walking dewater treatment needs.
The water dew point of pipeline natural gas is proposed in GB50251-2003 and is distinctly claimed：Water dew point should be than conveying bar
Minimum environment temperature is low 5 DEG C under part.This is just defeated to the natural gas of cold district (such as winter extreme value temperature is less than -25 DEG C of area)
Send and propose higher requirement.Therefore, cold district is in order to obtain the natural gas of low water dew point to ensure that the safety of natural gas is defeated
Send, it is necessary to which deep dehydration processing is carried out to natural gas.Water dew point reaches -100 DEG C before liquefied natural gas requires liquefaction, and this just needs
Deep dehydration processing is carried out using solid absorption method, and this method infrastructure investment is big, adsorbent reactivation high energy consumption, so in liquid
Change general use in the actual industrial production of natural gas and be segmented dehydration, deep dehydration is carried out to natural gas using triethylene glycol first,
Most water in natural gas are removed, its water dew point is reduced to less than -35 DEG C, then therein low contain is removed with solid absorption method
Water is measured, reaches required low dew-point temperature.In summary, in order to obtain the natural gas of low water dew point, new mistake is developed
Cheng Jiyue deep natural gas dewater treatment system and technique is extremely necessary.
And gas water dew point can only be down to using the system and technique that are proposed in above-mentioned patent CN201410490633-
18 DEG C, it is clear that the dewater treatment requirement of low water dew point natural gas can not be met.This is due within the system after gas dehydration
The aqueous dew point temperature that can reach substantially is to be determined that three is sweet by the regeneration triethylene glycol lean solution purity recycled in system
Alcohol regeneration purity is higher, and the gas water dew point after absorption system processing is lower.In system and technique that above-mentioned patent illustrates,
Triethylene glycol rich solution from absorption system carries out heat after obtaining heat heating by lean/rich liquid heat exchanger in hypergravity machine is regenerated
Regeneration, on the one hand due to being limited by heat exchanger heat exchange efficiency, temperature rise is insufficient, and on the other hand vapour-liquid is put down in by regeneration hypergravity machine
Bottleneck be present in the chemistry limitation of weighing apparatus, regeneration effect.Therefore, typically can only using the technique in the patent of invention in regenerative system
99.0% or so triethylene glycol lean solution is obtained, and uses the natural gas limit aqueous dew point temperature of lean solution progress absorption dewatering processing
It can only achieve about -18 DEG C, it is impossible to meet the deep dehydration processing requirement of low water dew point natural gas.
The content of the invention
The invention solves first technical problem be to provide a kind of deep natural gas dewatering system device；The device can
So that the purity of triethylene glycol lean solution after regeneration is brought up into 99.99wt%, using the triethylene glycol lean solution as absorbent, absorption can be made
Gas outlet water dew point through water suction processing in system is reduced to less than -35 DEG C, preferably can be to being down to less than -45 DEG C；So as to
Solve because of the low problem of gas dehydration depth in absorption system caused by triethylene glycol purity is not high, meet low water dew point natural gas
Dewater treatment requirement.Meanwhile gas dehydration and triethylene glycol regenerate two parts and use supergravity reactor, by strengthening gas
Liquid mass transfer, equipment size and investment are reduced, the natural gas processing requirement of the limited space occasion such as offshore platform can be met.
The invention solves second technical problem be to provide above-mentioned a kind of deep natural gas dewatering system device and de-
Water method.
To solve above-mentioned first technical problem, invention adopts the following technical scheme that：
A kind of deep natural gas dewatering system device of the present invention, including filter separator, the first hypergravity machine, condenser,
Lean/rich liquid heat exchanger, booster pump, surge tank, reboiler, the second hypergravity machine, flash tank, delivery pump, the first stop valve, second
Stop valve, the 3rd stop valve, the 4th stop valve, the 5th stop valve, pressure-reducing valve, flowmeter, vavuum pump, gas-liquid separator and threeway
Valve；
The outlet of the filter separator is connected with the gas phase import of the first hypergravity machine, the gas of first hypergravity machine
Mutually outlet is connected with the first stop valve import, and the first cut-off valve outlet leads to downstream section；After the first cut-off valve outlet
The 3rd stop valve, pressure-reducing valve and flowmeter, the outlet of flowmeter and the gas phase import of reboiler are sequentially connected in series on regeneration gas branch road
Connection；
The gaseous phase outlet of the reboiler is connected with the gas phase import of the second hypergravity machine, the gas of second hypergravity machine
Mutually outlet, the gas outlet of the surge tank and vacuum pump inlet three are connected with triple valve, be the second hypergravity machine by vavuum pump,
Reboiler, surge tank three provide subnormal ambient；The liquid-phase outlet of the reboiler leads to surge tank by the second stop valve and entered
Mouthful；
The gas phase import connection of the vacuum pump outlet and gas-liquid separator, the gaseous phase outlet of the gas-liquid separator lead to
Reboiler heats fuel as it；
The liquid-phase outlet of first hypergravity machine is connected with the rich solution import of lean/rich liquid heat exchanger, and the lean/rich liquid changes
The rich solution outlet of hot device is connected with flash tank import, and the gaseous phase outlet of the flash tank also leads to reboiler and is used as heating fuel,
The import of the liquid outlet and delivery pump of the flash tank connects, and the gaseous phase outlet of the flash tank is connected to gas-liquid separator；
The outlet of the delivery pump is connected with the fluid inlet of the second hypergravity machine, and the liquid-phase outlet of second hypergravity machine with boiling again
The fluid inlet connection of device, the reboiler liquid-phase outlet are connected through the second stop valve with surge tank import, the surge tank liquid
Mutually outlet be pressurized pump inlet is connected, the outlet of the booster pump is connected with the lean solution import of lean/rich liquid heat exchanger, it is described it is poor/
The lean solution outlet of rich solution heat exchanger is connected with condenser inlet, the outlet of the condenser and the fluid inlet of the first hypergravity machine
It is connected, realizes the circulation of triethylene glycol.
As the further improvement of technical scheme, on the pipeline that the vavuum pump connects with triple valve, the 4th section is additionally provided with
Only valve.
As the further improvement of technical scheme, the pipeline of gas-liquid separator is connected in the gaseous phase outlet of the flash tank
On, it is connected by branch line with triple valve, and branch line is provided with the 5th stop valve.
To solve above-mentioned second technical problem, the present invention utilizes the dehydration side of above-mentioned deep natural gas dewatering system device
Method, comprise the following steps：
1), pressure is that 2-10MPa natural gas _ raw material gas enters filter separator, removes free aqueous water and solid is miscellaneous
Matter, exported discharge by filter separator afterwards；
2), the natural gas _ raw material gas of discharge enters the first hypergravity machine in step 1), sweet with three in the first hypergravity machine
Alcohol lean solution counter current contacting is dehydrated, and the natural gas after dehydration discharges the first hypergravity machine, and a part is used as product gas, separately takes small part
As regeneration gas, regeneration gas is after pressure-reducing valve depressurizes, into reboiler；
3) the triethylene glycol rich solution after, being absorbed water in step 2) discharges the first hypergravity machine from the first hypergravity machine liquid outlet,
With entering flash tank after the heat exchange of triethylene glycol lean solution；
4), the regeneration gas entered in step 2) from reboiler bottom, from reboiler after being contacted in reboiler with triethylene glycol
The outlet discharge at top, into the second hypergravity machine；
5), the triethylene glycol in step 3) is pumped into the second hypergravity machine, the gas of the second hypergravity machine after flash tank flashes
Mutually outlet, the gas outlet of surge tank, vavuum pump three are connected by triple valve, are ended when opening the 4th stop valve and closing the 5th
During valve, vavuum pump provides single and stable subnormal ambient for the second hypergravity machine, reboiler and surge tank；It is pumped into step 3)
The regeneration gas that the triethylene glycol rich solution of second hypergravity machine is discharged with reboiler in step 4) counter current contacting under subnormal ambient regenerates；
Triethylene glycol lean solution after regeneration is discharged from the liquid-phase outlet of the second hypergravity machine；Regeneration gas is arranged from the second hypergravity machine gaseous phase outlet
Go out；
6) gas-liquid is entered after, being discharged in step 5) from the regeneration gas of the second hypergravity machine gaseous phase outlet discharge by vavuum pump
In separator, condensation can use after removing free liquid water as the heating fuel of reboiler；
7), reboiler is entered from the triethylene glycol lean solution of the second hypergravity machine outflow in step 5), and regeneration gas is secondary contacts
And fully discharged after concurrent heating from reboiler liquid-phase outlet；
8), the triethylene glycol lean solution that step 7) is discharged from reboiler liquid-phase outlet enters surge tank, is formed in surge tank steady
Determine liquid level；
9), the triethylene glycol lean solution in step 8) in surge tank is pumped into lean/rich liquid heat exchanger by being pressurized；In lean/rich liquid
Exchanged heat in heat exchanger with triethylene glycol rich solution in step 3), be again introduced into the first hypergravity machine after condenser condenses afterwards, it is real
The circulation of existing triethylene glycol.
As the further improvement of technical scheme, in step 2), the volume ratio of regeneration gas dosage and product gas is 1：1000-
1：10000.
As the further improvement of technical scheme, in step 2), the volume ratio of triethylene glycol lean solution and natural gas _ raw material gas is
1：5000~1：50000.
As the further improvement of technical scheme, the hypergravity level of the first hypergravity machine is 20-1000 in step 2), step
It is rapid 5) in the hypergravity level of the second hypergravity machine be 20-1000.
By the above-mentioned dewatering process of the present invention, triethylene glycol lean solution purity can reach 99.99wt% in step 2), use this
The triethylene glycol of purity carries out gas dehydration processing, and gas outlet dew point can reach less than -35 DEG C, minimum to be down to -45 DEG C
Below.
As the further improvement of technical scheme, the vacuum of the second hypergravity machine, reboiler and surge tank in step 5)
For 50-90kPa.
As the further improvement of technical scheme, in step 7), reboiler temperature is 160-204 DEG C.
As the further improvement of technical scheme, condenser temperature is 15-40 DEG C in step 9).
Any scope described in the present invention includes any numerical value and end value or end value between end value and end value
Between any subrange for being formed of any number.
Unless otherwise specified, each raw material in the present invention can be obtained by commercially available purchase, equipment used in the present invention
The conventional equipment in art or the prior art with reference to art can be used to carry out.
Compared with prior art, the present invention has the advantages that：
(1) it is high to be dehydrated depth.System and technique proposed by the present invention, in triethylene glycol regenerative system, develop new regeneration
Technique, it can be the abundant additional heat of rich solution regenerative process by the introducing of reboiler, promote it fully to regenerate；Pass through regeneration gas
Introduce, strengthen liquid phase turbulence in regeneration hypergravity machine, reduce water partial pressure in gas phase；Subnormal ambient is created by vavuum pump, promoted
Transfer of the water from liquid phase to gas phase, breaches the limitation of normal pressure hot recycling mode in original technique.Pass through system proposed by the present invention
The purity of triethylene glycol lean solution after regeneration can be brought up to 99.99wt% by system and technique, and absorption is used as using the triethylene glycol lean solution
Agent, the gas outlet water dew point through water suction processing in absorption system can be made to be reduced to less than -45 DEG C.
(2) it is applied widely.Present system is provided simultaneously with negative pressure intensifying regenerating and two kind three of regeneration gas intensifying regenerating is sweet
Alcohol renovation process, the system can select suitable triethylene glycol renovation process according to actual conditions, if will to gas dehydration processing
When asking not high, it can use and a kind of method therein is used alone, to reduce cost., can be simultaneously if dewater treatment requires higher
Using two methods, meet the gas dehydration process of different requirements.
(3) process is intensive.The natural gas that the regeneration gas introduced in the present invention is handled from system itself, without external agency
Add, the partial regeneration gas can not only be used as working media in addition, by strengthening liquid phase turbulence in triethylene glycol regenerative system
With the mode intensifying regenerating for reducing steam partial pressure, triethylene glycol lean solution purity is improved, can also after discharge regenerative system simple process
As the heating fuel of reboiler in system, that realizes system itself takes making full use of for heat and the energy, and process is intensive.
(4) Gas Dehydration System and triethylene glycol regenerative system two parts are reacted using hypergravity in present system
Device.Therefore, the system has the advantages of high-gravity technology itself concurrently：Greatly increase gas liquid interfacial area, improve gas-liquid mass transfer efficiency,
It is simple to operate, equipment size is small, driving and parking is easy, suitable for limited space region, such as offshore platform and offshore natural gas exploitation
Operation ship etc..
Brief description of the drawings
The embodiment of the present invention is described in further detail below in conjunction with the accompanying drawings
Fig. 1 is deep natural gas dewatering system device structural representation of the present invention；
Numeral mark in Fig. 1：
1- filter separators；The hypergravity machines of 2- first；3- condensers；The lean/rich liquid heat exchangers of 4-；
5- booster pumps；6- surge tanks；7- reboilers；The hypergravity machines of 8- second；
9- flash tanks；10- delivery pumps；The stop valves of 11- first；The stop valves of 12- second
The stop valves of 13- the 3rd；The stop valves of 19- the 4th；The stop valves of 20- the 5th；14- pressure-reducing valves；
15- flowmeters；16- vavuum pumps；17- gas-liquid separators；18- triple valves.
Embodiment
In order to illustrate more clearly of the present invention, with reference to preferred embodiment, the present invention is described further.Ability
Field technique personnel should be appreciated that following specifically described content is illustrative and be not restrictive, and this should not be limited with this
The protection domain of invention.
Shown in Figure 1, a kind of deep natural gas dewatering system device of the present invention, including filter separator 1, first are overweight
It is power machine 2, condenser 3, lean/rich liquid heat exchanger 4, booster pump 5, surge tank 6, reboiler 7, the second hypergravity machine 8, flash tank 9, defeated
Send pump 10, the first stop valve 11, the second stop valve 12, the 3rd stop valve 13, the 4th stop valve 19, the 5th stop valve 20, decompression
Valve 14, flowmeter 15, vavuum pump 16, gas-liquid separator 17 and triple valve 18；
The outlet of the filter separator 1 is connected with the gas phase import of the first hypergravity machine 2, first hypergravity machine 2
Gaseous phase outlet be connected with the import of the first stop valve 11, the first stop valve 11 outlet leads to downstream section；First stop valve
The 3rd stop valve 13, pressure-reducing valve 14 and flowmeter 15, the outlet of flowmeter 15 are sequentially connected in series on regeneration gas branch road behind 11 outlets
It is connected with the gas phase import of reboiler 7；
The gaseous phase outlet of the reboiler 7 is connected with the gas phase import of the second hypergravity machine 8, second hypergravity machine 8
Gaseous phase outlet, the surge tank 6 gas outlet and the import three of vavuum pump 16 be connected with triple valve 18, be the by vavuum pump 16
Two hypergravity machines 8, reboiler 7, the three of surge tank 6 provide subnormal ambient；The liquid-phase outlet of the reboiler 7 passes through the second cut-off
Valve 12 leads to the import of surge tank 6；
The outlet of vavuum pump 16 is connected with the gas phase import of gas-liquid separator 17, and the gas phase of the gas-liquid separator 17 goes out
Mouth leads to reboiler 7 and heats fuel as its；
The liquid-phase outlet of first hypergravity machine 2 is connected with the rich solution import of lean/rich liquid heat exchanger 4, the lean/rich liquid
The rich solution outlet of heat exchanger 4 is connected with the import of flash tank 9, and the gaseous phase outlet of the flash tank 9 also leads to reboiler 7 as heating
Fuel, the liquid outlet of the flash tank 9 are connected with the import of delivery pump 10, and the gaseous phase outlet of the flash tank 9 is connected to gas
Liquid/gas separator 17；The outlet of the delivery pump 10 is connected with the fluid inlet of the second hypergravity machine 8, second hypergravity machine 8
Liquid-phase outlet be connected with the fluid inlet of reboiler 7, the liquid-phase outlet of reboiler 7 is through the second stop valve 12 and surge tank 6
Import is connected, and the liquid-phase outlet of surge tank 6 is connected with the import of booster pump 5, and outlet and the lean/rich liquid of the booster pump 5 exchange heat
The lean solution import connection of device 4, the lean solution outlet of the lean/rich liquid heat exchanger 4 are connected with the import of condenser 3, the condenser 3
Outlet is connected with the fluid inlet of the first hypergravity machine 2, realizes the circulation of triethylene glycol.
As the further improvement of technical scheme, on the pipeline of the vavuum pump 16 and triple valve 18 connection, the is additionally provided with
Four stop valves 19.
As the further improvement of technical scheme, gas-liquid separator 17 is connected in the gaseous phase outlet of the flash tank 9
On pipeline, it is connected by branch line with triple valve 18, and branch line is provided with the 5th stop valve 20.
The present invention is comprised the following steps using the dewatering of above-mentioned deep natural gas dewatering system device：
1), pressure is that 2-10MPa natural gas _ raw material gas is passed through filter separator, and liquid therein is removed using gravitational settling
State water and solid impurity；
2), the natural gas _ raw material gas of discharge enters and enters the first hypergravity by the first hypergravity machine gas phase import in step 1)
Machine, triethylene glycol lean solution enter the first hypergravity machine by the fluid inlet of the first hypergravity machine, are uniformly injected in through liquid distribution trough
On the wire packing of hypergravity machine, triethylene glycol is moved from the inner ring of filler to outside circulation, and natural gas _ raw material gas is by the inside circulation of outer shroud
Dynamic, gas-liquid two-phase radially counter current contacting in packing layer, the water in natural gas _ raw material gas is absorbed by liquid phase triethylene glycol, after dehydration
Natural gas the first hypergravity machine is directly left by hypergravity machine gaseous phase outlet, a part is used as product gas, separately takes small part to make
For regeneration gas, regeneration gas is after pressure-reducing valve depressurizes, into reboiler；
3) the triethylene glycol rich solution after, being absorbed water in step 2) discharges the first hypergravity machine from the first hypergravity machine liquid outlet,
With entering flash tank after the heat exchange of triethylene glycol lean solution；
4), the regeneration gas entered in step 2) from reboiler bottom, from reboiler after being contacted in reboiler with triethylene glycol
The outlet discharge at top, into the second hypergravity machine；
5), the triethylene glycol in step 3) is pumped into the second hypergravity machine, the gas of the second hypergravity machine after flash tank flashes
Mutually outlet, the gas outlet of surge tank, vavuum pump three are connected by triple valve, are ended when opening the 4th stop valve and closing the 5th
During valve, vavuum pump provides single and stable subnormal ambient for the second hypergravity machine, reboiler and surge tank；It is pumped into step 3)
The regeneration gas that the triethylene glycol rich solution of second hypergravity machine is discharged with reboiler in step 4) counter current contacting under subnormal ambient regenerates；
Triethylene glycol lean solution after regeneration is discharged from the liquid-phase outlet of the second hypergravity machine；Regeneration gas is arranged from the second hypergravity machine gaseous phase outlet
Go out；
6) gas-liquid is entered after, being discharged in step 5) from the regeneration gas of the second hypergravity machine gaseous phase outlet discharge by vavuum pump
In separator, condensation can use after removing free liquid water as the heating fuel of reboiler；
7), reboiler is entered from the triethylene glycol lean solution of the second hypergravity machine outflow in step 5), and regeneration gas is secondary contacts
And fully discharged after concurrent heating from reboiler liquid-phase outlet；
8), the triethylene glycol lean solution that step 7) is discharged from reboiler liquid-phase outlet enters surge tank, is formed in surge tank
Stable liquid level；
9), the triethylene glycol lean solution in step 8) in surge tank is pumped into lean/rich liquid heat exchanger by being pressurized；In lean/rich liquid
Exchanged heat in heat exchanger with triethylene glycol rich solution in step 3), be again introduced into the first hypergravity machine after condenser condenses afterwards, it is real
The circulation of existing triethylene glycol.
In certain embodiments of the present invention, in step 2), the volume ratio of regeneration gas dosage and product gas is 1：1000-1：
10000, or 1：1000-1：2000, or 1：1000-1：3000, or 1：1000-1：4000, or 1：1000-1：5000, or 1：
1000-1：6000, or 1：1000-1：7000, or 1：1000-1：8000, or 1：1000-1：9000.
In certain embodiments of the present invention, in step 2), the volume ratio of triethylene glycol lean solution and natural gas _ raw material gas is 1：
5000-1：50000, or 1：5000-1：45000, or 1：5000-1：40000, or 1：5000-1：35000, or 1：5000-1：
30000, or 1：5000-1：25000, or 1：5000-1：20000, or 1：5000-1：15000, or 1：5000-1：10000.
In certain embodiments of the present invention, the hypergravity level of the first hypergravity machine is 20-1000 in step 2), or
50-1000, or 50-900, or 50-800, or 50-700, or 50-600, or 50-500, or 50-400, or 50-300, or 50-
200, or 50-100, or 100-1000, or 100-900, or 100-800, or 100-700, or 100-600, or 100-500, or
100-400, or 100-300, or 100-200, or 300-1000, or 300-900, or 300-800, or 300-700, or 300-
600, or 300-500, or 300-400；The hypergravity level of the second hypergravity machine in step 5) is 20-1000, or 50-
1000, or 50-900, or 50-800, or 50-700, or 50-600, or 50-500, or 50-400, or 50-300, or 50-200,
Or 50-100, or 100-1000, or 100-900, or 100-800, or 100-700, or 100-600, or 100-500, or 100-
400, or 100-300, or 100-200, or 300-1000, or 300-900, or 300-800, or 300-700, or 300-600, or
300-500, or 300-400.
By the above-mentioned dewatering process of the present invention, triethylene glycol lean solution purity can reach 99.99wt% in step 2), use this
The triethylene glycol of purity carries out gas dehydration processing, and gas outlet dew point can reach less than -35 DEG C, minimum to be down to -45 DEG C
Below.
In certain embodiments of the present invention, the vacuum of the second hypergravity machine, reboiler and surge tank is in step 5)
50-90kPa。
In certain embodiments of the present invention, in step 7), reboiler temperature is 160-204 DEG C.
In certain embodiments of the present invention, condenser temperature is 15-40 DEG C in step 9).
Embodiment 1
Negative pressure intensifying regenerating and regeneration gas intensifying regeneration are used simultaneously, it is sweet to carry out three using above-mentioned device and technique
Alcohol deep removal natural gas reclaimed water：The 3rd stop valve 13, the 4th stop valve 19 are opened, closes the 5th stop valve 20.
Gas pressure into the system is 7MPa, and the volume ratio of regeneration gas dosage and product gas is 1：2000, three is sweet
Alcohol lean solution and the volume ratio of natural gas _ raw material gas are 1：10000, the horizontal hypergravity of No.1 hypergravity machine is 200, and No. two overweight
The horizontal hypergravity of power machine is 200, vacuum 80kPa, 190 DEG C of reboiler temperature, and condenser temperature is 30 DEG C.This technique bar
Under part, triethylene glycol lean solution purity reaches 99.99wt% or so after regeneration, and export gas water dew point reaches less than -50 DEG C.
Embodiment 2
As described in Example 1, other conditions are constant, the hypergravity level of the first hypergravity machine are adjusted into 100, by this work
After skill processing, triethylene glycol lean solution purity reaches 99.99wt% or so after regeneration, and gas water dew point reaches less than -48 DEG C.
Embodiment 3
As described in Example 1, other conditions are constant, the hypergravity level of the first hypergravity machine are adjusted into 20, by this work
After skill processing, triethylene glycol lean solution purity reaches 99.99wt% or so after regeneration, and gas water dew point reaches less than -28 DEG C.
Embodiment 4
As described in Example 1, other conditions are constant, the hypergravity level of the second hypergravity machine are adjusted into 20, by this work
After skill processing, triethylene glycol lean solution purity reaches 99.86wt% or so after regeneration, and gas water dew point reaches less than -28 DEG C.
Embodiment 5
As described in Example 1, other conditions are constant, and the volume ratio of triethylene glycol lean solution and natural gas _ raw material gas is adjusted into 1：
20000, after this PROCESS FOR TREATMENT, triethylene glycol lean solution purity reaches 99.99wt% or so after regeneration, and gas water dew point reaches
To less than -35 DEG C.
Embodiment 6
As described in Example 1, other conditions are constant, and the volume ratio of regeneration gas dosage and product gas is adjusted into 1：10000, warp
After crossing this PROCESS FOR TREATMENT, triethylene glycol lean solution purity reaches 99.90wt% or so after regeneration, gas water dew point reach -36 DEG C with
Under.
Embodiment 7
As described in Example 1, other conditions are constant, and vacuum is adjusted into 60kPa, and after processing, triethylene glycol is poor after regeneration
Liquid purity reaches 99.93wt% or so, and gas water dew point reaches less than -38 DEG C.
Embodiment 8
As described in Example 1, other conditions are constant, and reboiler temperature is adjusted into 160 DEG C, and after processing, three is sweet after regeneration
Alcohol lean solution purity reaches 99.85wt% or so, and gas water dew point reaches less than -27 DEG C.
Embodiment 9
As described in Example 1, other conditions are constant, and condenser temperature is adjusted into 40 DEG C, after processing, triethylene glycol after regeneration
Lean solution purity reaches 99.99wt% or so, and gas water dew point reaches less than -30 DEG C.
Embodiment 10
Regeneration gas intensifying regenerating is used alone, is carried out using above-mentioned device and technique in triethylene glycol deep removal natural gas
Water.
As described in Example 1, other conditions are constant, open the 3rd stop valve 13, the 5th stop valve 20, close the 4th cut-off
Valve 19, now vacuum is 0kPa, and after treatment, triethylene glycol lean solution purity reaches 99.86wt% or so, natural gas after regeneration
Water dew point reaches less than -34 DEG C.
Embodiment 11
Negative pressure intensifying regenerating is used alone, is carried out using above-mentioned device and technique in triethylene glycol deep removal natural gas
Water：
As described in Example 1, other conditions are constant, open the 4th stop valve 19, close the 3rd stop valve 13 and the 5th section
Only valve 20, now regeneration gas dosage is 0m3/ h, through later, triethylene glycol lean solution purity reaches 99.70wt% or so, day after regeneration
Right air water dew point reaches less than -28 DEG C.
Comparative example 1
Both regenerated without using negative pressureization, also entered without using regeneration gas intensifying regeneration using above-mentioned device and technique
Row triethylene glycol deep removal natural gas reclaimed water：
As described in Example 1, other conditions are constant, open the 5th stop valve 20, close the 3rd stop valve 13 and the 4th section
Only valve 19, now without regeneration gas, vacuum 0kPa, after treatment, triethylene glycol lean solution purity reaches 98.85wt% after regeneration
Left and right, gas water dew point reach less than -16 DEG C.
Obviously, the above embodiment of the present invention is only intended to clearly illustrate example of the present invention, and is not pair
The restriction of embodiments of the present invention.For those of ordinary skill in the field, may be used also on the basis of the above description
To make other changes in different forms.Here all embodiments can not be exhaustive.It is every to belong to this hair
Row of the obvious changes or variations that bright technical scheme is extended out still in protection scope of the present invention.
Claims (10)
- A kind of 1. deep natural gas dewatering system device, it is characterised in that：Including filter separator (1), the first hypergravity machine (2), condenser (3), lean/rich liquid heat exchanger (4), booster pump (5), surge tank (6), reboiler (7), the second hypergravity machine (8), Flash tank (9), delivery pump (10), the first stop valve (11), the second stop valve (12), the 3rd stop valve (13), the 4th stop valve (19), the 5th stop valve (20), pressure-reducing valve (14), flowmeter (15), vavuum pump (16), gas-liquid separator (17) and triple valve (18)；The outlet of the filter separator (1) is connected with the gas phase import of the first hypergravity machine (2), first hypergravity machine (2) gaseous phase outlet is connected with the first stop valve (11) import, and the first stop valve (11) outlet leads to downstream section；Described first The 3rd stop valve (13), pressure-reducing valve (14) and flowmeter (15) are sequentially connected in series on regeneration gas branch road behind stop valve (11) outlet, The outlet of flowmeter (15) is connected with the gas phase import of reboiler (7)；The gaseous phase outlet of the reboiler (7) is connected with the gas phase import of the second hypergravity machine (8), second hypergravity machine (8) gaseous phase outlet, the gas outlet of the surge tank (6) and vavuum pump (16) import three is connected with triple valve (18), by true Empty pump (16) is the second hypergravity machine (8), reboiler (7), surge tank (6) three provide subnormal ambient；The reboiler (7) Liquid-phase outlet leads to surge tank (6) import by the second stop valve (12)；Vavuum pump (16) outlet is connected with the gas phase import of gas-liquid separator (17), the gas phase of the gas-liquid separator (17) Outlet leads to reboiler (7) and heats fuel as it；The liquid-phase outlet of first hypergravity machine (2) is connected with the rich solution import of lean/rich liquid heat exchanger (4), the lean/rich liquid The rich solution outlet of heat exchanger (4) is connected with flash tank (9) import, and the gaseous phase outlet of the flash tank (9) also leads to reboiler (7) As heating fuel, the liquid outlet of the flash tank (9) is connected with the import of delivery pump (10), the gas of the flash tank (9) Mutually outlet is connected to gas-liquid separator (17)；The outlet of the delivery pump (10) connects with the fluid inlet of the second hypergravity machine (8) Connect, the liquid-phase outlet of second hypergravity machine (8) is connected with the fluid inlet of reboiler (7), and reboiler (7) liquid phase goes out Mouth is connected through the second stop valve (12) with surge tank (6) import, and surge tank (6) liquid-phase outlet connects with booster pump (5) import Connect, the outlet of the booster pump (5) is connected with the lean solution import of lean/rich liquid heat exchanger (4), the lean/rich liquid heat exchanger (4) Lean solution outlet is connected with condenser (3) import, the outlet of the condenser (3) and the fluid inlet phase of the first hypergravity machine (2) Connection.
- 2. deep natural gas dewatering system device according to claim 1, it is characterised in that：Preferably, the vavuum pump (16) and on the pipeline of triple valve (18) connection, it is additionally provided with the 4th stop valve (19).
- 3. deep natural gas dewatering system device according to claim 1, it is characterised in that：Preferably, in the flash tank (9) gaseous phase outlet is connected on the pipeline of gas-liquid separator (17), is connected by branch line with triple valve (18), and branch Pipeline is provided with the 5th stop valve (20).
- 4. using the dewatering of any deep natural gas dewatering system device in the claims 1-3, its feature exists In comprising the following steps：1), pressure is that 2-10MPa natural gas _ raw material gas is passed through filter separator, and aqueous water therein is removed using gravitational settling And solid impurity；2), the natural gas _ raw material gas of discharge enters and enters the first hypergravity machine by the first hypergravity machine gas phase import in step 1), Triethylene glycol lean solution enters the first hypergravity machine by the fluid inlet of the first hypergravity machine, is uniformly injected in through liquid distribution trough overweight On the wire packing of power machine, triethylene glycol is moved from the inner ring of filler to outside circulation, and natural gas _ raw material gas is moved by the inside circulation of outer shroud, gas Liquid two-phase radially counter current contacting in packing layer, the water in natural gas _ raw material gas are absorbed by liquid phase triethylene glycol, the day after dehydration Right gas directly leaves the first hypergravity machine by hypergravity machine gaseous phase outlet, and a part is used as product gas, separately takes small part as again Anger, regeneration gas is after pressure-reducing valve depressurizes, into reboiler；3) the triethylene glycol rich solution after, being absorbed water in step 2) discharges the first hypergravity machine from the first hypergravity machine liquid outlet, with three Enter flash tank after the heat exchange of glycol lean solution；4), the regeneration gas entered in step 2) from reboiler bottom, after being contacted in reboiler with triethylene glycol at the top of reboiler Outlet discharge, into the second hypergravity machine；5), the triethylene glycol in step 3) is pumped into the second hypergravity machine after flash tank flashes, and the gas phase of the second hypergravity machine goes out Mouth, the gas outlet of surge tank, vavuum pump three are connected by triple valve, when the 4th stop valve of opening and close the 5th stop valve When, vavuum pump provides single and stable subnormal ambient for the second hypergravity machine, reboiler and surge tank；Is pumped into step 3) The regeneration gas that the triethylene glycol rich solution of two hypergravity machines is discharged with reboiler in step 4) counter current contacting under subnormal ambient regenerates；Again Triethylene glycol lean solution after life is discharged from the liquid-phase outlet of the second hypergravity machine；Regeneration gas is arranged from the second hypergravity machine gaseous phase outlet Go out；6) gas-liquid separation is entered after, being discharged in step 5) from the regeneration gas of the second hypergravity machine gaseous phase outlet discharge by vavuum pump In device, condensation can use after removing free liquid water as the heating fuel of reboiler；7), reboiler is entered from the triethylene glycol lean solution of the second hypergravity machine outflow in step 5), and regeneration gas is secondary contacts and fill After dividing concurrent heating, discharged from reboiler liquid-phase outlet；8), the triethylene glycol lean solution that step 7) is discharged from reboiler liquid-phase outlet enters surge tank, and stabilizing solution is formed in surge tank Position；9), the triethylene glycol lean solution in step 8) in surge tank is pumped into lean/rich liquid heat exchanger by being pressurized；Exchanged heat in lean/rich liquid Exchanged heat in device with triethylene glycol rich solution in step 3), be again introduced into the first hypergravity machine after condenser condenses afterwards, realize three The circulation of glycol.
- 5. dewatering according to claim 4, it is characterised in that：Preferably, in step 2), regeneration gas dosage and product gas Volume ratio be 1：1000-1：10000, or 1：1000-1：2000, or 1：1000-1：3000, or 1：1000-1：4000, or 1： 1000-1：5000, or 1：1000-1：6000, or 1：1000-1：7000, or 1：1000-1：8000, or 1：1000-1：9000.
- 6. dewatering according to claim 4, it is characterised in that：Preferably, in step 2), triethylene glycol lean solution and natural gas The volume ratio of unstripped gas is 1：5000-1：50000, or 1：5000-1：45000, or 1：5000-1：40000, or 1：5000-1： 35000, or 1：5000-1：30000, or 1：5000-1：25000, or 1：5000-1：20000, or 1：5000-1：15000, or 1：5000-1：10000.
- 7. dewatering according to claim 4, it is characterised in that：Preferably, in step 2), the first hypergravity machine it is overweight Power level is 20-1000, or 50-1000, or 50-900, or 50-800, or 50-700, or 50-600, or 50-500, or 50- 400, or 50-300, or 50-200, or 50-100, or 100-1000, or 100-900, or 100-800, or 100-700, or 100-600, or 100-500, or 100-400, or 100-300, or 100-200, or 300-1000, or 300-900, or 300- 800, or 300-700, or 300-600, or 300-500, or 300-400；In step 5), the hypergravity of the second hypergravity machine is horizontal For 20-1000, or 50-1000, or 50-900, or 50-800, or 50-700, or 50-600, or 50-500, or 50-400, or 50-300, or 50-200, or 50-100, or 100-1000, or 100-900, or 100-800, or 100-700, or 100-600, Or 100-500, or 100-400, or 100-300, or 100-200, or 300-1000, or 300-900, or 300-800, or 300- 700, or 300-600, or 300-500, or 300-400.
- 8. dewatering according to claim 4, it is characterised in that：Preferably, the second hypergravity machine, reboiler in step 5) Vacuum with surge tank is 50-90kPa.
- 9. dewatering according to claim 4, it is characterised in that：Preferably, in step 7), reboiler temperature 160- 204℃。
- 10. dewatering according to claim 4, it is characterised in that：Preferably, condenser temperature is 15-40 in step 9) ℃。
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