CN105969439A - Low-temperature condensate treatment process and device for natural gas treatment plant deoiling and dewatering device - Google Patents
Low-temperature condensate treatment process and device for natural gas treatment plant deoiling and dewatering device Download PDFInfo
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- CN105969439A CN105969439A CN201610397419.4A CN201610397419A CN105969439A CN 105969439 A CN105969439 A CN 105969439A CN 201610397419 A CN201610397419 A CN 201610397419A CN 105969439 A CN105969439 A CN 105969439A
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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
-
- 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
Abstract
The invention discloses a low-temperature condensate treatment process for a natural gas treatment plant deoiling and dewatering device. The process includes the following steps that 1, the temperature is increased to 29 DEG C after low-temperature condensate is preheated twice; 2, the low-temperature condensate is separated into gas-phase gas, alcohol-containing water and unstable gas condensate through a three-phase separator; 3, the alcohol-containing water is output to a methyl alcohol recycling device; 4, the unstable gas condensate enters a gas condensate stabilizing tower after being preheated and is heated to 142 DEG C at the tower bottom with conduction oil after being stabilized, the saturated vapor pressure reaches 70 kPa, the temperature is decreased to 40 DEG C after cooling is performed twice, and the stabilized gas condensate is output to a product tank field; 5, the gas-phase gas is mixed with tower top noncondensable gas to generate phase-change cooling, the temperature of the mixed gas is reduced to -10 DEG C, the mixed gas is subjected to low-temperature gas-liquid separation, the hydrocarbon dew point of fuel gas meets the quality requirement, and a liquid phase flows back to the top of the stabilizing tower. The invention further provides a device for implementing the process. Low-temperature separation of mixed gas is achieved under the condition that no external cold supply source is available, and thus investment is reduced; the requirement for cooling high-temperature gas condensate is met under the condition that an air cooler is omitted; besides, the energy of heat flow is reasonably utilized.
Description
Technical field
The present invention devises a kind of natural gas processing plant deoiling, dewatering device low temperature and coagulates liquor treating process, and implements to be somebody's turn to do
The device of technique.
Background technology
The low temperature lime set of natural gas processing plant's deoiling, dewatering device takes off from the low temperature gas-liquid separator of this device, removing oil
Water device uses the condensation at low temperature separating technology of propane refrigeration, meets the requirement of simultaneously deoiling, dewatering, containing saturation water and
The raw natural gas of a small amount of lighter hydrocarbons is after deoiling, dewatering device processes, and the water dew point of product natural gas, hydrocarbon dew point meet
The requirement of national standard " natural gas " GB 17820, the low temperature lime set that cryogenic separation goes out contains water, does not stablizes condensation
Oil, methanol and the natural gas of dissolving.Deoiling, dewatering device worst cold case is by injecting methanol with under suppression cryogenic conditions
The generation of hydrate.
The processing method of low temperature lime set generally uses following two method:
(1) by heating, blood pressure lowering, three phase separation, gas phase gas produces as centre as fuel gas, oil phase-condensate
Product export trade, aqueous phase-recycle containing methanol-water.The method technique is simple, and energy consumption is low, invests low, seldom uses；
(2) by heating, blood pressure lowering, three phase separation, condensate is through fractionation stabilization, and three phase separation gas phase gas is with steady
Carry out back as international sale, methanol-water directly as fuel gas, stabilized condensate after determining the mixing of tower overhead gas fixed gas
Receipts process；The method is current prevailing technology, technology maturation.
Both the above method there is problems in that
(1) in the fuel gas of method one, liquid hydrocarbon content is higher, goes out liquid hydrocarbon in fuel gas system condensation, causes system to run
Unstable and there is potential safety hazard, the saturated vapor pressure of condensate can not meet the requirement of corresponding specification；
(2) in the fuel gas of method two, liquid hydrocarbon content is higher, goes out liquid hydrocarbon in fuel gas system condensation, causes system to run
Unstable and there is potential safety hazard.
Summary of the invention
It is an object of the invention to solve a large amount of lime set of fuel gas system in prior art separate out, low temperature lime set produces
Outer row's gaseous mixture can not meet the requirement of fuel gas hydrocarbon dew point, to this end, the present invention provides a kind of natural gas processing plant
Low temperature coagulate liquor treating process and implement the device of this technique.
The technical solution used in the present invention is as follows:
1., low temperature lime set preheats in one-level gas-liquid heat-exchange step through condensate stabilization column overhead fixed gas, low temperature
The temperature of lime set raises, and tower top fixed gas cools down through low temperature lime set simultaneously, and temperature reduces；
Step 2., step 1. preheat after low temperature lime set in two grades of gas-liquid heat-exchanges through high-temperature stable condensate second
Secondary preheating, temperature rises to 29 DEG C；
3., the low temperature lime set after secondary preheating is separated into gas phase gas, containing alcohol water through three phase separator and does not stablizes step
Condensate；
4., the containing alcohol water that 3. step produces exports to methanol recovery device step through pipeline；
5., the non-stabilized condensate that 3. step produces high-temperature stable condensate in liquid-liquid heat exchanger preheats step,
Temperature raises and enters into condensate stabilization tower epimere, is forming stabilized condensate, at the bottom of tower at the bottom of the tower of condensate stabilization tower
Stabilized condensate high temperature heat conductive oil in reboiler be heated to 142.7 DEG C, formed high-temperature stable condensate；High temperature is steady
Determining the cooling for the first time of the condensate non-stabilized condensate in liquid-liquid heat exchanger, temperature declines, through two grades of gas-liquid heat exchanges
Low temperature lime set cooling twice in device, temperature drops to 40 DEG C again, the high-temperature stable condensate output after cooling twice
To product tank field；
6., the gas phase gas that 3. step produces is formed with the condensate stabilization tower 7 tower top fixed gas after cooling and mixes step
Gas, produces freezing by change of state, and mixture temperature is reduced to-10 DEG C；Gaseous mixture enters cold catch pot and carries out gas-liquid separation,
The liquid produced flow to condensate stabilization column overhead by low-temperature oil blowback；Its hydrocarbon dew point of fuel gas produced meets combustion
Material gas quality requirements, exports to fuel gas system through pipeline.
The low temperature lime set that step is 1. described, its temperature is-15 DEG C, and pressure is 5.5MPa, consists of C1～C11+、
Water and methanol, wherein the mole percent level of water is 16%, and the mole percent level of methanol is 19%, C6+
Mole percent level be 46.44%, the mole percent level of C1～C5 fixed gas is 18.56%.
The condensate stabilization column overhead fixed gas that step is 1. described, its temperature is 45 DEG C, and pressure 0.4MPa consists of
C1～C11 +And saturation water, wherein the mole percent level of saturation water is 4.92%, C1～C5Molar percentage contain
Amount is 93.62%, C6 +Mole percent level be 1.46%.
Preheating that step is 1. described and cooling, make use of heat and the cold of low temperature lime set of tower top fixed gas simultaneously,
Low temperature lime set temperature is risen to 2 DEG C by-15 DEG C, and tower top fixed gas temperature is reduced to-5 DEG C by 45 DEG C；Step is 5. described
Heating and for the first time cooling, make use of cold and the heat of high-temperature stable condensate of non-stabilized condensate simultaneously,
Non-stabilized condensate temperature is risen to 65 DEG C by 29 DEG C, and high-temperature stable condensate temperature is reduced to 109 DEG C by 142 DEG C；
The second time that second time preheats and step is the 5. described cooling that step is 2. described, make use of the cold of low temperature lime set simultaneously
With the heat of high-temperature stable condensate, low temperature lime set 1 temperature is risen to 29 DEG C by 2 DEG C, high-temperature stable condensation oil temperature
Degree is reduced to 40 DEG C by 109 DEG C.
The 5. described stabilized condensate of step forms reboiling through high temperature heat conductive oil heating, through repeatedly gas in reboiler
Liquid mass transfer fractional distillation, the temperature making the high-temperature stable condensate formed at the bottom of condensate stabilization tower tower is 142 DEG C, saturated vapor
Pressure reaches 70kPa.
The 6. described gaseous mixture of step enters low temperature gas-liquid separator and carries out during gas-liquid separation needs at cryogenic conditions (-10
DEG C～-20 DEG C) under carry out, to guarantee that the hydrocarbon dew point of gaseous mixture meets the requirement of fuel gas, liquid is back to tower top.
A kind of natural gas processing plant deoiling, dewatering device low temperature lime set processing means, it at least includes one-level gas-liquid heat exchange
Device, two grades of gas-liquid heat-exchanges and three phase separator, low temperature lime set carries pipe by the low temperature lime set being provided with block valve
Line is connected with the import of three phase separator after sequentially passing through described one-level gas-liquid heat-exchange, two grades of gas-liquid heat-exchanges,
The outlet of three phase separator is provided with three tunnels, respectively gaseous phase outlet, oil phase outlet and aqueous phase outlet,
A kind of natural gas processing plant deoiling, dewatering device low temperature lime set processing means also includes liquid-liquid heat exchanger, condensate
Stabilizer, cold catch pot and low temperature oil pump, described three phase separator aqueous phase exports by being provided with containing alcohol water liquid
Level control valve is connected with methanol recovery device with the containing alcohol water feed-line of block valve；Oil phase exports by being provided with not
The not steady condensate feed-line of steady condensate effusion meter and the first fluid level control valve is steady with condensate through liquid-liquid heat exchanger
The middle and upper part import determining tower is connected, and is provided with reboiler at the bottom of condensate stabilization tower tower, and reboiler passes through stabilized condensate
Feed-line is sequentially through liquid-liquid heat exchanger, two grades of gas-liquid heat-exchanges, stabilized condensate effusion meter, second Liquid level
Valve is connected with product tank field；Three phase separator gaseous phase outlet is defeated by the gas phase gas being provided with three phase separator pressure valve
Sending pipeline blended letter shoot line to be connected with the import of cold catch pot, the outlet of cold catch pot has two-way: gas
Outlet and liquid-phase outlet mutually, gaseous phase outlet is provided by pipeline and the fuel gas system of fuel gas stream gauge and block valve
System is connected, and liquid-phase outlet is connected to condensate stabilization column overhead by low-temperature oil feed-line through low temperature oil pump.
Described condensate stabilization tower passes through tower top fixed gas feed-line through one-level gas-liquid heat-exchange and tower pressure control valve
Connect on mixed gas pipeline line with gas phase letter shoot line afterwards.
Being provided with heating coil in described three phase separator, high temperature heat conductive oil passes through conduction oil feed-line through blocking
Valve, heating coil, conduction oil flow control valve are connected with reboiler import, and reboiler outlet is carried by conduction oil
Pipeline returns with low temperature conduction oil through block valve and is connected.
Beneficial effects of the present invention:
Liquor treating process and device is coagulated: first can by the low temperature of natural gas processing plant's deoiling, dewatering device of the present invention
So that outer row's gaseous mixture that low temperature lime set produces reaches the requirement of fuel gas hydrocarbon dew point, solve fuel gas system a large amount of
The problem that lime set separates out, improves stability and safety；Second saturated vapor that simultaneously can make stabilized condensate
Pressure reaches code requirement；Under conditions of 3rd supplies low-temperature receiver outside, it is achieved that the cryogenic separation of gaseous mixture, save
Give low-temperature receiver outside, reduce investment；4th under conditions of cancelling air cooler, meets the cooling to high temperature condensate；
5th, the energy of Appropriate application hot-fluid, reduce the thermic load of reboiler, energy-saving effect is notable.
Below with reference to the accompanying drawing explanation to preferred embodiment, the above-mentioned and other objects, features and advantages of the present invention
Will be apparent from.
Accompanying drawing explanation
Fig. 1 is that the low temperature of natural gas processing plant's deoiling, dewatering device of the present invention coagulates the technological process of liquor treating process and shows
It is intended to.
Description of reference numerals:
1-low temperature lime set, 2-low temperature lime set feed-line, 3-one-level gas-liquid heat-exchange, 4-bis-grades of gas-liquid heat-exchanges, 5-
Three phase separator, 6-liquid-liquid heat exchanger, 7-condensate stabilization tower, 8-reboiler, 9-cold catch pot, 10-low-temperature oil
The not steady condensate feed-line of pump, 11-not steady condensate effusion meter, 12-the first fluid level control valve, 13-, 14-are stable
Condensate feed-line, 15-tower top fixed gas feed-line, 16-gas phase letter shoot line, 17-mixed gas pipeline
Line, 18-heating coil, 19-stabilized condensate effusion meter, 20-the second fluid level control valve, 21-containing alcohol water feed-line,
22-low-temperature oil feed-line, 23-methanol recovery device, 24-high temperature heat conductive oil, 25-low temperature conduction oil return, 26-fuel
Air-flow gauge, 27-fuel gas system, 28-containing alcohol water fluid level control valve, 29-conduction oil feed-line, 30-conduction oil
Flow control valve, 31-three phase separator pressure valve, 32-tower pressure control valve.
Detailed description of the invention
The present invention is described more fully below is embodied as case.It should be noted that, the embodiments described herein is served only for
Illustrate, be not limited to the present invention.
Embodiment 1:
A kind of natural gas processing plant deoiling, dewatering device low temperature coagulates liquor treating process, comprises the following steps:
1., low temperature lime set 1 preheats in one-level gas-liquid heat-exchange 3 step through condensate stabilization tower 7 tower top fixed gas,
The temperature of low temperature lime set 1 raises, and tower top fixed gas cools down through low temperature lime set 1 simultaneously, and temperature reduces；
Step 2., step 1. preheat after low temperature lime set 1 in two grades of gas-liquid heat-exchanges 4 through high-temperature stable condensate
Second time preheating, temperature rises to 29 DEG C；
3., the low temperature lime set 1 after secondary preheating is separated into gas phase gas, containing alcohol water and not through three phase separator 5 to step
Stabilized condensate；
4., the containing alcohol water that 3. step produces exports to methanol recovery device 23 step through pipeline；
5., the non-stabilized condensate that 3. step produces high-temperature stable condensate in liquid-liquid heat exchanger 6 preheats step,
Temperature raises and enters into condensate stabilization tower 7 epimere, is forming stabilized condensate at the bottom of the tower of condensate stabilization tower 7,
Stabilized condensate at the bottom of tower high temperature heat conductive oil 24 in reboiler 8 is heated to 142.7 DEG C, forms high-temperature stable condensation
Oil；The cooling for the first time of the high-temperature stable condensate non-stabilized condensate in liquid-liquid heat exchanger 6, temperature declines, warp
Low temperature lime set 1 cooling twice in two grades of gas-liquid heat-exchanges 4, temperature drops to 40 DEG C again, the height after cooling twice
Temperature stabilized condensate exports to product tank field；
6., the gas phase gas that 3. step produces is formed with the condensate stabilization tower 7 tower top fixed gas after cooling and mixes step
Gas, produces freezing by change of state, and mixture temperature is reduced to-10 DEG C；Gaseous mixture entrance cold catch pot 9 carries out gas-liquid and divides
From, the liquid of generation is back to condensate stabilization tower 7 tower top by low temperature oil pump 10；Its hydrocarbon of the fuel gas dew produced
Point meets fuel gas quality requirements, exports to fuel gas system 27 through pipeline.
Present invention also offers the low temperature for above-mentioned natural gas processing plant deoiling, dewatering device to coagulate liquor treating process and be able to
The device implemented, as it is shown in figure 1, it at least includes one-level gas-liquid heat-exchange 3, two grades of gas-liquid heat-exchanges 4 and three-phases
Separator 5, low temperature lime set 1 sequentially passes through described one-level by being provided with the low temperature lime set feed-line 2 of block valve
It is connected with the import of three phase separator 5 after 3, two grades of gas-liquid heat-exchanges 4 of gas-liquid heat-exchange, going out of three phase separator 5
Mouth is provided with three tunnels, respectively gaseous phase outlet, oil phase outlet and aqueous phase outlet.
A kind of natural gas processing plant deoiling, dewatering device low temperature lime set processing means also includes liquid-liquid heat exchanger 6, condensate
Stabilizer 7, cold catch pot 9 and low temperature oil pump 10, described three phase separator 5 aqueous phase exports by being provided with
Containing alcohol water fluid level control valve 28 is connected with methanol recovery device 23 with the containing alcohol water feed-line 21 of block valve；Oil phase
Export the not steady condensate feed-line by being provided with not steady condensate effusion meter 11 and the first fluid level control valve 12
13 are connected with the middle and upper part import of condensate stabilization tower 7 through liquid-liquid heat exchanger 6, install at the bottom of condensate stabilization tower 7 tower
Reboiler 8, reboiler 8 is had to pass through stabilized condensate feed-line 14 sequentially through 6, two grades of gas-liquids of liquid-liquid heat exchanger
Heat exchanger 4, stabilized condensate effusion meter the 19, second fluid level control valve 20 are connected with product tank field；Three phase separator
5 gaseous phase outlets are by being provided with the blended letter shoot line of gas phase letter shoot line 16 of three phase separator pressure valve 31
17 are connected with the import of cold catch pot 9, and the outlet of cold catch pot 9 has a two-way: gaseous phase outlet and liquid-phase outlet,
Gaseous phase outlet is provided by fuel gas stream gauge 26 and is connected with fuel gas system 27 with the pipeline of block valve, liquid phase
Outlet is connected to condensate stabilization tower 7 tower top by low-temperature oil feed-line 22 through low temperature oil pump 10.
This example is as follows in the operating procedure of the low temperature lime set processing means of natural gas processing plant's deoiling, dewatering device:
Step is 1.: treatment plant's deoiling, dewatering device is carried out low temperature lime set 1 and carried by the low temperature lime set being provided with block valve
Pipeline 2 enters in one-level gas-liquid heat-exchange 3 and preheats through condensate stabilization tower 7 tower top fixed gas, low temperature lime set 1
Temperature is risen to 2 DEG C by-15 DEG C, and tower top fixed gas cools down through low temperature lime set 1 in one-level gas-liquid heat-exchange 3 simultaneously,
The temperature of condensate stabilization tower 7 tower top fixed gas is reduced to-5 DEG C by 45 DEG C；
Step is 2.: the low temperature lime set 1 after preheating is in low temperature lime set feed-line 2 enters two grades of gas-liquid heat-exchanges 4
Completing second time through high-temperature stable condensate to preheat, the temperature of low temperature lime set 1 is risen to 29 DEG C by 2 DEG C；
Step is 3.: the low temperature lime set 1 after secondary preheating enters three phase separator 5, warp through low temperature lime set feed-line 2
Three phase separator 5 is separated into gas phase gas, containing alcohol water and non-stabilized condensate；
Step is 4.: the containing alcohol water of three phase separator 5 aqueous phase outlet exports to Methanol Recovery through containing alcohol water feed-line 21
Device 23；
Step is 5.: the non-stabilized condensate of three phase separator 5 oil phase outlet is entered by steady condensate feed-line 13
Entering in liquid-liquid heat exchanger 6 and preheat through high-temperature stable condensate, the temperature of not steady condensate is risen to 65 DEG C by 29 DEG C,
Not steady condensate after preheating is by not steady condensate feed-line 13 and condensate stabilization tower 7 middle and upper part import phase
Even；Forming stabilized condensate at the bottom of the tower of condensate stabilization tower 7, the stabilized condensate at the bottom of tower is high in reboiler 8
Temperature conduction oil 24 is heated to 142.7 DEG C, forms high-temperature stable condensate；Entered by stabilized condensate feed-line 14
Entering through not steady condensate cooling for the first time in liquid-liquid heat exchanger 6, the temperature of high-temperature stable condensate is reduced to by 142 DEG C
109℃；High-temperature stable condensate after cooling enters two grades of gas-liquid heat-exchanges 4 by stabilized condensate feed-line 14
Middle through low temperature lime set 1 second time cooling, the temperature of stabilized condensate is reduced to 40 DEG C by 109 DEG C；After reducing temperature twice
Stabilized condensate reach code requirement, can be as international sale, stabilized condensate is through stabilized condensate effusion meter 19
Exported to product tank field by stabilized condensate feed-line 14 with the second fluid level control valve 20.
Step is 6.: condensate stabilization tower 7 tower top after the gas phase gas of three phase separator 5 gaseous phase outlet and cooling does not coagulates
Gas forms gaseous mixture, produces freezing by change of state, and mixture temperature is reduced to-10 DEG C, and tower top fixed gas temperature is by-5 DEG C of falls
As little as-10 DEG C, the temperature of three phase separator 5 gas phase gas is reduced to-10 DEG C by 29 DEG C.Gaseous mixture is carried by gaseous mixture
Pipeline 17 enters cold catch pot 9 and carries out gas-liquid separation, and the fuel gas hydrocarbon dew point of generation meets fuel gas quality requirements,
Fuel gas exports to fuel gas system 27 by being provided with the pipeline of fuel gas stream gauge 26 and block valve；The liquid produced
Body is back to condensate stabilization tower 7 by low-temperature oil feed-line 22 through low temperature oil pump 10.
The low temperature of natural gas processing plant's deoiling, dewatering device of the present invention coagulates liquor treating process and device, permissible
The outer row's gaseous mixture making low temperature lime set produce reaches the requirement of fuel gas hydrocarbon dew point, solves fuel gas system and coagulates in a large number
The problem that liquation goes out, improves stability and safety；The saturated vapor pressure simultaneously making stabilized condensate reaches specification
Requirement.
Embodiment 2:
On the basis of embodiment 1, described low temperature lime set, its temperature is-15 DEG C, and pressure is 5.5MPa, composition
For C1～C11 +, water and methanol, wherein water content is 16% (mol), and Methanol Molar content is 19% (mol),
C6 +Content is 46.44% (mol), C1～C5Fixed gas content is 18.56% (mol).
Described condensate stabilization tower 7 tower top fixed gas, its temperature is 45 DEG C, and pressure 0.4MPa consists of C1~
C11 +And saturation water, wherein saturation water content is 4.92% (mol), C1～C5Content is 93.62% (mol), C6 +
Content is 1.46% (mol).
Preheating that step is 1. described and cooling, make use of heat and the cold of low temperature lime set 1 of tower top fixed gas simultaneously,
Low temperature lime set 1 temperature is risen to 2 DEG C by-15 DEG C, and tower top fixed gas temperature is reduced to-5 DEG C by 45 DEG C；Step 5. institute
The heating stated and for the first time cooling, make use of cold and the heat of high-temperature stable condensate of non-stabilized condensate simultaneously,
Non-stabilized condensate temperature is risen to 65 DEG C by 29 DEG C, and high-temperature stable condensate temperature is reduced to 109 DEG C by 142 DEG C；
The second time that second time preheats and step is the 5. described cooling that step is 2. described, make use of the cold of low temperature lime set 1 simultaneously
Amount and the heat of high-temperature stable condensate, low temperature lime set 1 temperature is risen to 29 DEG C by 2 DEG C, high-temperature stable condensate
Temperature is reduced to 40 DEG C by 109 DEG C.
Described three phase separator 5, completes, to low temperature lime set 1 three phase separation after heating, to create gas phase gas, contain
Alcohol water and non-stabilized condensate.
Described liquid-liquid heat exchanger 6, has preheated non-stabilized condensate while reducing stabilized condensate temperature, has reduced
The heating load of conduction oil, has saved energy.
The low temperature of natural gas processing plant's deoiling, dewatering device provided by the present invention coagulates liquor treating process and device, first
First under conditions of low-temperature receiver outside, it is achieved that the cryogenic separation of gaseous mixture, save outer to low-temperature receiver, reduced
Investment；Secondly, under conditions of cancelling air cooler, the cooling to high temperature condensate is met；Furthermore, Appropriate application heat
The energy of stream, reduces the thermic load of reboiler, and energy-saving effect is notable.
Embodiment 3
On the basis of embodiment 1, the 6. described tower top fixed gas of step mixes with three phase separator gas phase gas, by
Lime set in the two vapor liquid equilibrium again, wherein part lime set evaporation endothermic, form temperature fall, make gaseous mixture
Temperature is less than tower top fixed gas before mixing and the three phase separator respective temperature of gas phase gas.Gaseous mixture enters low temperature gas-liquid
When separator 9 carries out gas-liquid separation, needs are carried out at cryogenic conditions-10 DEG C～-20 DEG C, to guarantee that the hydrocarbon of gaseous mixture reveals
Point meets the requirement of fuel gas, and liquid is back to tower top.
The 5. described stabilized condensate of step heats formation reboiling in reboiler 8 through high temperature heat conductive oil 24, through too much
Secondary gas-liquid mass transfer fractional distillation, the temperature making the high-temperature stable condensate formed at the bottom of condensate stabilization tower 7 tower is 142 DEG C, full
Reaching 70kPa with vapour pressure, high temperature heat conductive oil 24 is passed through in described gas-liquid mass transfer fractional distillation, i.e. stabilized condensate at the bottom of tower
Part vaporization in reboiler 8 after heating, the gas of rising and the liquid countercurrent contact mass transfer fractional distillation of decline, thus
The saturated vapor pressure making stabilized condensate reaches requirement.
Embodiment 4:
On the basis of above-described embodiment, described condensate stabilization tower 7 is by tower top fixed gas feed-line 15 warp
One-level gas-liquid heat-exchange 3 is connected in mixed gas pipeline line with gas phase letter shoot line 16 with after tower pressure control valve 32
On 17.
Being provided with heating coil 18 in described three phase separator 5, high temperature heat conductive oil 24 is by conduction oil feed-line
29 are connected with reboiler 8 import through block valve, heating coil 18, conduction oil flow control valve 30, reboiler 8
Outlet is returned 25 through block valve with low temperature conduction oil by conduction oil feed-line 29 and is connected.
This example at the concrete operation step of the low temperature lime set processing means of natural gas processing plant's deoiling, dewatering device is:
Step is 1.: treatment plant's deoiling, dewatering device is carried out low temperature lime set 1 and carried by the low temperature lime set being provided with block valve
Pipeline 2 enters in one-level gas-liquid heat-exchange 3 and preheats through condensate stabilization tower 7 tower top fixed gas, low temperature lime set 1
Temperature is risen to 2 DEG C by-15 DEG C, and tower top fixed gas cools down through low temperature lime set 1 in one-level gas-liquid heat-exchange 3 simultaneously,
The temperature of condensate stabilization tower 7 tower top fixed gas is reduced to-5 DEG C by 45 DEG C；
Step is 2.: the low temperature lime set 1 after preheating is in low temperature lime set feed-line 2 enters two grades of gas-liquid heat-exchanges 4
Completing second time through high-temperature stable condensate to preheat, the temperature of low temperature lime set 1 is risen to 29 DEG C by 2 DEG C；
Step is 3.: the low temperature lime set 1 after secondary preheating enters three phase separator 5, warp through low temperature lime set feed-line 2
Three phase separator 5 is separated into gas phase gas, containing alcohol water and non-stabilized condensate；
Step is 4.: the containing alcohol water of three phase separator 5 aqueous phase outlet exports to Methanol Recovery through containing alcohol water feed-line 21
Device 23；
Step is 5.: the non-stabilized condensate of three phase separator 5 oil phase outlet is entered by steady condensate feed-line 13
Entering in liquid-liquid heat exchanger 6 and preheat through high-temperature stable condensate, the temperature of not steady condensate is risen to 65 DEG C by 29 DEG C,
Not steady condensate after preheating is by not steady condensate feed-line 13 and condensate stabilization tower 7 middle and upper part import phase
Even；Forming stabilized condensate at the bottom of the tower of condensate stabilization tower 7, the stabilized condensate at the bottom of tower is high in reboiler 8
Temperature conduction oil 24 is heated to 142.7 DEG C, forms high-temperature stable condensate；Entered by stabilized condensate feed-line 14
Entering through not steady condensate cooling for the first time in liquid-liquid heat exchanger 6, the temperature of high-temperature stable condensate is reduced to by 142 DEG C
109℃；High-temperature stable condensate after cooling enters two grades of gas-liquid heat-exchanges 4 by stabilized condensate feed-line 14
Middle through low temperature lime set 1 second time cooling, the temperature of stabilized condensate is reduced to 40 DEG C by 109 DEG C；After reducing temperature twice
Stabilized condensate reach code requirement, can be as international sale, stabilized condensate is through stabilized condensate effusion meter 19
Exported to product tank field by stabilized condensate feed-line 14 with the second fluid level control valve 20.
Step is 6.: condensate stabilization tower 7 tower top after the gas phase gas of three phase separator 5 gaseous phase outlet and cooling does not coagulates
Gas forms gaseous mixture, produces freezing by change of state, and mixture temperature is reduced to-10 DEG C, and tower top fixed gas temperature is by-5 DEG C of falls
As little as-10 DEG C, the temperature of three phase separator 5 gas phase gas is reduced to-10 DEG C by 29 DEG C.Gaseous mixture is carried by gaseous mixture
Pipeline 17 enters cold catch pot 9 and carries out gas-liquid separation, and the fuel gas hydrocarbon dew point of generation meets fuel gas quality requirements,
Fuel gas exports to fuel gas system 27 by being provided with the pipeline of fuel gas stream gauge 26 and block valve；The liquid produced
Body is back to condensate stabilization tower 7 by low-temperature oil feed-line 22 through low temperature oil pump 10.
High temperature heat conductive oil 24 is after the heating coil 18 in three phase separator 5 heats in the present embodiment, by leading
Hot oil transfer pipeline 29 enters thermal-stable condensate in reboiler 8, makes the stabilized condensate at the bottom of tower at reboiler 8
Interior part vaporizes, the gas of rising and the liquid countercurrent contact mass transfer fractional distillation of decline, so that the temperature of stabilized condensate
Degree raises, and the temperature of high temperature heat conductive oil 24 declines, and is exported to low temperature through block valve by conduction oil feed-line 29
Conduction oil returns at 25 mouthfuls.
Parts that the present embodiment describes the most in detail and structure belong to the well-known components of the industry and common structure or conventional hands
Section, describes the most one by one.
Claims (10)
1. natural gas processing plant's deoiling, dewatering device low temperature coagulates liquor treating process, it is characterised in that include
Following steps:
Step 1., low temperature lime set (1) in one-level gas-liquid heat-exchange (3) through condensate stabilization tower (7)
Tower top fixed gas preheats, and the temperature of low temperature lime set (1) raises, and tower top fixed gas coagulates through low temperature simultaneously
Liquid (1) cools down, and temperature reduces；
Step 2., step 1. preheat after low temperature lime set (1) warp in two grades of gas-liquid heat-exchanges (4)
The second time preheating of high-temperature stable condensate, temperature rises to 29 DEG C；
3., the low temperature lime set (1) after secondary preheating is separated into gas phase through three phase separator (5) to step
Gas, containing alcohol water and non-stabilized condensate；
4., the containing alcohol water that 3. step produces is through pipeline output to methanol recovery device (23) for step；
Step 5., the non-stabilized condensate that 3. step produces high-temperature stable in liquid-liquid heat exchanger (6)
Condensate preheats, and temperature raises and enters into condensate stabilization tower (7) epimere, in condensate stabilization tower (7)
Tower at the bottom of formed stabilized condensate, the stabilized condensate at the bottom of tower is high temperature heat conductive oil (24) in reboiler (8)
It is heated to 142.7 DEG C, forms high-temperature stable condensate；High-temperature stable condensate is through liquid-liquid heat exchanger (6)
In for the first time cooling of non-stabilized condensate, temperature declines, low temperature in two grades of gas-liquid heat-exchanges (4)
Lime set (1) cooling twice, temperature drops to 40 DEG C again, the high-temperature stable condensate after cooling twice
Output is to product tank field；
Step 6., the gas phase gas that 3. step produces with cooling after condensate stabilization tower (7) tower top do not coagulate
Gas forms gaseous mixture, produces freezing by change of state, and mixture temperature is reduced to-10 DEG C；Gaseous mixture enters low temperature
Separator (9) carries out gas-liquid separation, and the liquid of generation is back to condensate by low temperature oil pump (10)
Stabilizer (7) tower top；Its hydrocarbon dew point of fuel gas produced meets fuel gas quality requirements, defeated through pipeline
Go out to fuel gas system (27).
2. science and engineering at a kind of natural gas processing plant as claimed in claim 1 deoiling, dewatering device low temperature lime set
Skill, it is characterised in that: the low temperature lime set (1) that step is 1. described, its temperature is-15 DEG C, and pressure is
5.5MPa, consists of C1～C11+, water and methanol, wherein the mole percent level of water is 16%,
The mole percent level of methanol is 19%, C6+Mole percent level be 46.44%, C1～C5
The mole percent level of fixed gas is 18.56%.
3. science and engineering at a kind of natural gas processing plant as claimed in claim 1 deoiling, dewatering device low temperature lime set
Skill, it is characterised in that: condensate stabilization tower (7) the tower top fixed gas that step is 1. described, its temperature is
45 DEG C, pressure 0.4MPa, consist of C1～C11 +And saturation water, the wherein molar percentage of saturation water
Content is 4.92%, C1～C5Mole percent level be 93.62%, C6 +Mole percent level
It is 1.46%.
4. science and engineering at a kind of natural gas processing plant as claimed in claim 1 deoiling, dewatering device low temperature lime set
Skill, it is characterised in that: preheating that step is 1. described and cooling, make use of the heat of tower top fixed gas simultaneously
Amount and the cold of low temperature lime set (1), low temperature lime set (1) temperature is risen to 2 DEG C by-15 DEG C, tower top
Fixed gas temperature is reduced to-5 DEG C by 45 DEG C；Heating and first time that step is 5. described cool down, profit simultaneously
With cold and the heat of high-temperature stable condensate of non-stabilized condensate, non-stabilized condensate temperature by
29 DEG C rise to 65 DEG C, and high-temperature stable condensate temperature is reduced to 109 DEG C by 142 DEG C；Step is 2. described
Second time preheating and the 5. described second time cooling of step, make use of simultaneously low temperature lime set cold and
The heat of high-temperature stable condensate, low temperature lime set (1) temperature is risen to 29 DEG C by 2 DEG C, high-temperature stable
Condensate temperature is reduced to 40 DEG C by 109 DEG C.
5. science and engineering at a kind of natural gas processing plant as claimed in claim 1 deoiling, dewatering device low temperature lime set
Skill, it is characterised in that: the 5. described stabilized condensate of step through high temperature heat conductive oil (24) heating at weight
Boiling device (8) is formed reboiling, through repeatedly gas-liquid mass transfer fractional distillation, makes condensate stabilization tower (7) tower
The temperature of the high-temperature stable condensate that the end is formed is 142 DEG C, and saturated vapor pressure reaches 70kPa.
6. science and engineering at a kind of natural gas processing plant as claimed in claim 1 deoiling, dewatering device low temperature lime set
Skill, it is characterised in that: the 6. described gaseous mixture of step enters low temperature gas-liquid separator (9) and carries out gas-liquid
Need during separation to carry out under cryogenic conditions (-10 DEG C～-20 DEG C), full to guarantee the hydrocarbon dew point of gaseous mixture
The requirement of foot fuel gas, liquid is back to tower top.
7. natural gas processing plant's deoiling, dewatering device low temperature lime set processing means, it is characterised in that: it is extremely
Include one-level gas-liquid heat-exchange (3), two grades of gas-liquid heat-exchanges (4) and three phase separator (5) less, low
Temperature lime set (1) sequentially passes through described by being provided with low temperature lime set feed-line (2) of block valve
One-level gas-liquid heat-exchange (3), two grades of gas-liquid heat-exchanges (4) afterwards with the import of three phase separator (5)
Being connected, the outlet of three phase separator (5) is provided with three tunnels, respectively gaseous phase outlet, oil phase outlet and
Aqueous phase exports.
8. a kind of natural gas processing plant as claimed in claim 7 deoiling, dewatering device low temperature lime set processes dress
Put, it is characterised in that: it also includes that liquid-liquid heat exchanger (6), condensate stabilization tower (7), low temperature divide
From device (9) and low temperature oil pump (10), described three phase separator (5) aqueous phase exports by being provided with
Containing alcohol water feed-line (21) of containing alcohol water fluid level control valve (28) and block valve fills with Methanol Recovery
Put (23) to be connected；Oil phase outlet is by being provided with not steady condensate effusion meter (11) and the first liquid level
The not steady condensate feed-line (13) of control valve (12) is steady with condensate through liquid-liquid heat exchanger (6)
The middle and upper part import determining tower (7) is connected, and is provided with reboiler (8) at the bottom of condensate stabilization tower (7) tower,
Reboiler (8) by stabilized condensate feed-line (14) sequentially through liquid-liquid heat exchanger (6), two grades
Gas-liquid heat-exchange (4), stabilized condensate effusion meter (19), the second fluid level control valve (20) and product
Tank field is connected；Three phase separator (5) gaseous phase outlet is by being provided with three phase separator pressure valve (31)
The entering of gas phase letter shoot line (16) blended letter shoot line (17) and cold catch pot (9)
Mouthful being connected, the outlet of cold catch pot (9) has a two-way: gaseous phase outlet and liquid-phase outlet, gaseous phase outlet
It is provided by fuel gas stream gauge (26) to be connected with fuel gas system (27) with the pipeline of block valve,
Liquid-phase outlet is connected to condensate stabilization by low-temperature oil feed-line (22) through low temperature oil pump (10)
Tower (7) tower top.
9. a kind of natural gas processing plant as claimed in claim 8 deoiling, dewatering device low temperature lime set processes dress
Put, it is characterised in that: described condensate stabilization tower (7) passes through tower top fixed gas feed-line (15)
Connect with gas phase letter shoot line (16) after one-level gas-liquid heat-exchange (3) and tower pressure control valve (32)
Lead on mixed gas pipeline line (17).
10. a kind of natural gas processing plant as claimed in claim 7 deoiling, dewatering device low temperature lime set processes dress
Put, it is characterised in that: it is provided with heating coil (18), high temperature in described three phase separator (5)
Conduction oil (24) passes through conduction oil feed-line (29) through block valve, heating coil (18), heat conduction
Oil flow control valve (30) is connected with reboiler (8) import, and heat conduction is passed through in reboiler (8) outlet
Oil feed-line (29) goes back to (25) through block valve with low temperature conduction oil and is connected.
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