CN205874316U - Condensate desulfurization stabilising arrangement - Google Patents
Condensate desulfurization stabilising arrangement Download PDFInfo
- Publication number
- CN205874316U CN205874316U CN201620846091.5U CN201620846091U CN205874316U CN 205874316 U CN205874316 U CN 205874316U CN 201620846091 U CN201620846091 U CN 201620846091U CN 205874316 U CN205874316 U CN 205874316U
- Authority
- CN
- China
- Prior art keywords
- condensate
- desulfurization
- phase
- stabilizer
- stabilized
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a condensate desulfurization stabilising arrangement, including the not steady state condensate flash tank that connects gradually, not steady state condensate filter, one -level heat exchanger, three -phase separator, second grade heat exchanger, condensate desulfurization stabilization tower, bottom reboiler and steady state condensate delivery pump. The utility model has the advantages that: let in condensate stabilization desulfurizing tower bottom as air stripping gas with fuel gas, will stablely contain in the sulphur condensate with partial organic sulfur desorption, adopt simultaneously to carry and heat up in a steamer the light component desorption of technology in with the condensate, make hydrogen sulfide content and saturated steam in the product condensate press requirements such as satisfying the national standard. Simultaneously the utility model discloses still divide into direct current method and reposition of redundant personnel method according to desulfurization stabilization tower's feeding method difference, the condensate processing apparatus of processing scale >= 100 ton / day adopts the reposition of redundant personnel method more economical, and the direct current method more is applicable to the device of handling the small scale.
Description
Technical field
This utility model relates to a kind of method utilizing stripping and stripping to combine by light component contained in condensate, sulfuration
Hydrogen and the device of part organic sulfur removal.
Background technology
Condensate refers to from gas condensate field or oil field associated natural gas condensation liquid phase component out, also known as natural vapour
Oil.The hydro carbons that in natural gas, part is heavier under the high temperature, condition of high voltage of oil reservoir in gas phase state, due to pressure and temperature during gas production
Degree reduce, these heavier hydro carbons from natural gas condensation and go out, become light oil (title condensate).Its main component is C5Extremely
C8The mixture of hydro carbons, and containing a small amount of more than C8Hydro carbons and hydrogen sulfide, thiophene-based, thio-alcohol, thioether class and vulcanize more
The impurity such as thing, its fraction is many at 20 DEG C～200 DEG C, and proportion is less than 0.78, and the content ratio of its heavy hydrocarbon and non-hydrocarbon component is former
Oil is low, and volatility is good.Broadly, isolated condensate from gas well well site and natural gas processing plant's gas phase treatment facility
Belonging to gas reducing liquid, condensate, not directly as product, needs to carry out stabilized treatment, and removing affects the saturated steaming of condensate
The lighter hydrocarbons of vapour pressure are to control the saturated vapor pressure of condensate.For sulphur-containing condensate oil, due to H2The poisoning of S burn into and sour crude oil
The problems such as storage tank spontaneous combustion occur, condensate is in addition to removing light component, in addition it is also necessary to it is carried out desulfurization process.
Conventional sulphur-containing condensate oil processes technique and is respectively process for stabilizing and sulfur removal technology, and process for stabilizing predominantly reduces
Its saturated vapor pressure, common process is blood pressure lowering heating flash evaporation and stripping technique, for stabilized condensate and remove part H2S.To the greatest extent
Pipe is stripped of the H of part2S, but the H in stabilized condensate2S content is still unsatisfactory for requirement, needs to carry out follow-up desulfurization work
Skill.Conventional sulfur removal technology mainly has stripping, adsorbs, extracts, aoxidizes and aoxidize-extraction process.Stripping process refers to steaming
Vapour is as compositions such as stripping gas, hydrogen sulfide contained in removing condensate；Absorbing process have 13X molecular sieve adsorption technique and
IRVAD technique removing sulfur component；Extraction process has caustic extraction technology and N mono-N-formyl morpholine N (NFM) extraction technique；Oxidation has secondary
Sodium chlorate oxidation technology and NO2Oxidation technology；Oxidation-extraction technique is exactly oxidation technology and extraction technique desulfurization altogether
Technique, the most relatively common have liquid-liquid sulfur removal technology, conventional fixed bed deodorizing technology, low alkali number Minalk fixed bed desulfurization work
Skill, the catalyst fixed bed doctor treatment of Merox-10 and without caustic alkali Merox sulfur removal technology.
Condensate after stably desulphurizing processes can be directly used as fuel, and is the quality raw materials of petroleum refining industry, Ke Yifen
Separate out the petrochemicals such as ethane, propane, butane, light oil or gasoline.The Condensate Field that the whole world has been found that at present exceedes
More than 12200, it is distributed mainly on the U.S., Russia, Australia, the Central Asia and the Middle East and the Asian-Pacific area.Current domestic condensate
The place of production is mainly distributed on Tarim Oilfield, Zhongyuan Oil Field, oil field, the East Sea etc., and especially Tarim Oilfield, condensate in place accounts for entirely
The 80% of state's gross reserves.Along with a large amount of exploitations of whole world natural gas resource, condensate desulfurization process for stabilizing has become natural gas and has added
Work and an important component part of process.
Summary of the invention
This utility model overcomes shortcoming of the prior art, it is provided that a kind of condensate desulfurization stabilising arrangement, by condensation
Oil is stable and desulfurization realizes in a condensate desulfurization stabilizer, and uses fuel gas (to be mainly composed of methane CH4) make
For H contained in gas stripping gas removing condensate2S and part organic sulfur.Process technique of the present utility model is more energy efficient, more environmentally friendly,
Reduce running cost and cost of investment.
The technical solution of the utility model is: a kind of condensate desulfurization stabilising arrangement, the most stably coagulates including be sequentially connected with
Analysis oil flash tank, non-stabilized condensate filter, first-class heat exchanger, three phase separator, secondary heat exchanger, condensate desulfurization are stablized
Tower and bottom reboiler；Stabilized condensate outlet at the bottom of described condensate desulfurization stabilizer tower, secondary heat exchanger, first-class heat exchanger
It is sequentially connected with stabilized condensate delivery pump；The gaseous phase outlet pipeline of described non-stabilized condensate flash tank is arranged unstable
Condensate flash tank gaseous pressure regulation valve；The gaseous phase outlet pipeline of three phase separator arranges three phase separator gaseous pressure
Regulation valve；Condensate desulfurization stabilizer top gaseous phase outlet conduit arranges the regulation of condensate desulfurization stabilizer top gas phase pressure
Valve；Condensate desulfurization stabilizer lower end gas stripping gas inlet duct arranges gas stripping gas flow control valve；In bottom reboiler heat
Flow rate of heat medium regulation valve is set on matchmaker's outlet conduit.
Compared with prior art, the utility model has the advantages that: by the stripping process for stabilizing in condensate stabilization technique with
Stripping process in sulfur removal technology combines and is optimized, and designs a kind of novel desulfurization stabilising arrangement, this device according to
The difference of desulfurization stabilizer feeding manner is divided into shunting and direct current method.Condensate desulfurization stabilising arrangement by flash tank, filter,
First-class heat exchanger, three phase separator, secondary heat exchanger, condensate desulfurization stabilizer, bottom reboiler and condensate delivery pump
Composition.Technique initially with blood pressure lowering heating flash evaporation removes the light component of a part in condensate, steady subsequently into condensate desulfurization
Determining tower, employing stripping technique is by the lights removal in condensate, simultaneously from the H being passed through at the bottom of tower gas stripping gas removing condensate2S
With part organic sulfur, thus reach meet requirement stabilized condensate.This device can remove it while stabilized condensate
H contained by2S and part organic sulfur, energy-saving and emission-reduction, reduce running cost, reduce one-time investment, concrete manifestation is as follows:
(1) this device passes through air stripping and stripping technique, it is possible to the light component in removing condensate and H effectively2S, permissible
The saturated vapor pressure of condensate is down to below 68kPa, H2S content is down to below 50ppm, thus obtains and meet stablizing of requirement
Condensate.
(2) for the condensate processing means for the treatment of scale >=100 ton day, this device is by using shunting feeding manner
Condensate desulfurization stabilizer is fed, improves the efficiency of heat and mass, improve condensate product volume, thus obtain more
Economic benefit.For small-scale condensate processing means, the product yield that shunting is obtained with direct current method is almost identical.Therefore
Shunting can be used for large-scale condensate processing means, direct current is then used for small-scale condensate processing means
Method is the most economical reliable.
(3) sulfur removal technology of traditional process for stabilizing and improvement is combined, reduce the one of whole condensate processing means
The investment of secondary property and operating cost.
Accompanying drawing explanation
This utility model will illustrate by example and with reference to the appended drawing, wherein:
Fig. 1 is the condensate desulfurization process for stabilizing flow chart of direct current method；
Fig. 2 is the condensate desulfurization process for stabilizing flow chart of shunting.
Detailed description of the invention
A kind of condensate desulfurization stabilising arrangement, as depicted in figs. 1 and 2, including: non-stabilized condensate flash tank 1, stable
Condensate filter 2, first-class heat exchanger 3, three phase separator 4, secondary heat exchanger 5, condensate desulfurization stabilizer 6 are (to fill out in figure
Material tower as a example by, plate column can be used), bottom reboiler 7, stabilized condensate delivery pump 8, non-stabilized condensate flash tank liquid phase
Liquid level adjusting valve 9, non-stabilized condensate flash tank gaseous pressure regulation valve 10, three phase separator oil phase Liquid level adjusting valve 11, three
Top gaseous phase pressure is stablized in phase separator aqueous phase Liquid level adjusting valve 12, three phase separator gaseous pressure regulation valve 13, condensate desulfurization
Liquid phase Liquid level adjusting valve 15, gas stripping gas flow control valve 16, flow rate of heat medium regulation at the bottom of force regulating valve 14, condensate desulfurization stabilizer
Valve 17 and condensate stabilization tower feed stream adjustable valve 18 (being only used for Fig. 2 shunting technique) etc., wherein:
Non-stabilized condensate flash tank 1, non-stabilized condensate filter 2, first-class heat exchanger 3, three phase separator 4, two grades
Heat exchanger 5, condensate desulfurization stabilizer 6 and bottom reboiler 7 are sequentially connected with；Stablizing at the bottom of condensate desulfurization stabilizer 6 tower is solidifying
Analysis oil export, secondary heat exchanger 5, first-class heat exchanger 3 and stabilized condensate delivery pump 8 are sequentially connected with；
The liquid-phase outlet pipeline of non-stabilized condensate flash tank 1 arranges non-stabilized condensate flash tank liquid phase liquid level adjust
Joint valve 9；The gaseous phase outlet pipeline of non-stabilized condensate flash tank 1 arranges the regulation of non-stabilized condensate flash tank gaseous pressure
Valve 10；The oil phase outlet pipe road of three phase separator 4 arranges three phase separator oil phase Liquid level adjusting valve 11；At three phase separator
Three phase separator aqueous phase Liquid level adjusting valve 12 is set on the aqueous phase outlet conduit of 4；On the gaseous phase outlet pipeline of three phase separator 4
Three phase separator gaseous pressure regulation valve 13 is set；Condensate desulfurization stabilizer 6 top gaseous phase outlet conduit arranges condensation
Oil desulfurization stabilizer top gas phase pressure regulation valve 14；It is stable that condensate desulfurization is set on stabilized condensate delivery pump 8 outlet conduit
Tower bottom liquid phase Liquid level adjusting valve 15；Condensate desulfurization stabilizer 6 tower lower end gas stripping gas inlet duct arranges gas stripping gas flow
Regulation valve 16；Bottom reboiler 7 heating agent outlet conduit arranges flow rate of heat medium regulation valve 17；
For the direct current method feeding manner shown in Fig. 1: the oil phase after three phase separator 4 separates is through secondary heat exchanger
Feed from condensate desulfurization stabilizer 6 upper inlet after 5 heat exchange；
For the shunting feeding manner shown in Fig. 2: the oil phase part after three phase separator 4 separates is through two grades
Feed from condensate desulfurization stabilizer 6 centre inlet (i.e. entrance 2) after heat exchanger 5 heat exchange；Another part directly takes off from condensate
Sulfur stabilizer 6 upper inlet (i.e. entrance 1) feeds, and arranges condensate stabilization tower feed stream adjustable valve on this inlet duct
18。
The operation principle of this device is: this device mainly includes two parts, and the blood pressure lowering flash distillation that Part I is traditional divides
From, Part II is that stripping is stablized and flashed vapour air stripping disengagement section.Non-stabilized condensate is first in non-stabilized condensate flash distillation
Carrying out the blood pressure lowering flash separation of the first order in tank 1, isolated liquid phase enters in three phase separator 4 after filtering and heating blood pressure lowering
Carry out second level heating blood pressure lowering flash separation.After double flash evaporation separates, most light component and part H2S is from condensate
In separate and become flashed vapour and process to other treatment facility, this is traditional condensate stabilization technological principle of Part I.
From three phase separator, oil phase liquid storage section condensate out enters condensate desulfurization stabilizer, adds through reboiler
Heat and mass in heat and condensate tower, according to the character that different component boiling point is different, by complete for the light component in condensate
Removing；Be passed through gas stripping gas in tower bottom, fuel gas system the fuel gas provided is as gas stripping gas simultaneously.The principle of air stripping desulfurization
As follows: air stripping desulfurization is a kind of physical process, mainly after methane enters condensate stabilization tower, it destroys in former stabilizer solidifying
The gas-liquid two-phase balance of analysis oil, makes biphase dividing potential drop all reduce, then the gas-liquid in condensate all spreads in gas stripping gas, but
Due to H2S and light phase organic sulfur with the composition in gas stripping gas more closely, so substantial amounts of H2S and light phase organic sulfur composition to
Gas phase spreads, to set up a new vapor-liquid equilibrium relationship, thus reaches to separate H2S and the purpose of light phase organic sulfur.Therefore work as
Gas stripping gas is from bottom to up by desulfurization stabilizer, almost all of H2S and most organic sulfur are stripped the band of gas and walk, thus reach
To removing H2The requirement of S.
This device is to be combined with traditional sulfur removal technology by tradition process for stabilizing and improved, and is possible not only to reduce life
Production capacity consumes, and increases product yield, it is also possible to reduce equipment one-time investment, reduces pollutant discharge amount, makes at condensate stabilization
Science and engineering skill develops towards accurate, green direction.
Claims (6)
1. a condensate desulfurization stabilising arrangement, it is characterised in that: the non-stabilized condensate flash tank that includes being sequentially connected with, the most steady
Determine condensate filter, first-class heat exchanger, three phase separator, secondary heat exchanger, condensate desulfurization stabilizer and bottom reboiler；
Stabilized condensate outlet, secondary heat exchanger, first-class heat exchanger and stabilized condensate at the bottom of described condensate desulfurization stabilizer tower are defeated
Pump is sent to be sequentially connected with；
The gaseous phase outlet pipeline of described non-stabilized condensate flash tank arranges non-stabilized condensate flash tank gaseous pressure adjust
Joint valve；The gaseous phase outlet pipeline of three phase separator arranges three phase separator gaseous pressure regulation valve；Steady in condensate desulfurization
Determine on column overhead gaseous phase outlet pipeline, to arrange condensate desulfurization stabilizer top gas phase pressure regulation valve；At condensate desulfurization stabilizer
On the gas stripping gas inlet duct of lower end, gas stripping gas flow control valve is set；Bottom reboiler heating agent outlet conduit arranges heating agent stream
Adjustable valve.
A kind of condensate desulfurization stabilising arrangement the most according to claim 1, it is characterised in that: separate through three phase separator
After oil phase after secondary heat exchanger heat exchange from condensate desulfurization stabilizer upper inlet feed.
A kind of condensate desulfurization stabilising arrangement the most according to claim 1, it is characterised in that: separate through three phase separator
After oil phase a part after secondary heat exchanger heat exchange from condensate desulfurization stabilizer centre inlet feed；Another part is direct
Feed from condensate desulfurization stabilizer upper inlet.
A kind of condensate desulfurization stabilising arrangement the most according to claim 3, it is characterised in that: at condensate desulfurization stabilizer
Condensate stabilization tower feed stream adjustable valve is set on upper inlet pipeline.
A kind of condensate desulfurization stabilising arrangement the most according to claim 1, it is characterised in that: in non-stabilized condensate flash distillation
Non-stabilized condensate flash tank liquid phase Liquid level adjusting valve is set on the liquid-phase outlet pipeline of tank；Oil phase at three phase separator exports
Three phase separator oil phase Liquid level adjusting valve is set on pipeline；The aqueous phase outlet conduit of three phase separator arranges three phase separator
Aqueous phase Liquid level adjusting valve；Liquid phase liquid level regulation at the bottom of condensate desulfurization stabilizer is set on stabilized condensate delivery pump outlet conduit
Valve.
A kind of condensate desulfurization stabilising arrangement the most according to claim 1, it is characterised in that: described condensate desulfurization is stable
Tower is packed tower or plate column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620846091.5U CN205874316U (en) | 2016-08-05 | 2016-08-05 | Condensate desulfurization stabilising arrangement |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620846091.5U CN205874316U (en) | 2016-08-05 | 2016-08-05 | Condensate desulfurization stabilising arrangement |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205874316U true CN205874316U (en) | 2017-01-11 |
Family
ID=57702007
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620846091.5U Active CN205874316U (en) | 2016-08-05 | 2016-08-05 | Condensate desulfurization stabilising arrangement |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205874316U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010637A (en) * | 2016-08-05 | 2016-10-12 | 中国石油集团工程设计有限责任公司 | Condensate oil desulphurization stabilizing apparatus and method thereof |
| CN109722267A (en) * | 2017-10-31 | 2019-05-07 | 珠海市启夏能源科技有限公司 | A kind of tower tank combined type condensate gasification system and its production technology |
-
2016
- 2016-08-05 CN CN201620846091.5U patent/CN205874316U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010637A (en) * | 2016-08-05 | 2016-10-12 | 中国石油集团工程设计有限责任公司 | Condensate oil desulphurization stabilizing apparatus and method thereof |
| CN106010637B (en) * | 2016-08-05 | 2017-11-28 | 中国石油集团工程设计有限责任公司 | A kind of condensate desulfurization stabilising arrangement and process |
| CN109722267A (en) * | 2017-10-31 | 2019-05-07 | 珠海市启夏能源科技有限公司 | A kind of tower tank combined type condensate gasification system and its production technology |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7678263B2 (en) | Gas stripping process for removal of sulfur-containing components from crude oil | |
| CN107922854B (en) | Method for LPG recovery | |
| CN205874316U (en) | Condensate desulfurization stabilising arrangement | |
| CN110180202A (en) | The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range | |
| CN103333056B (en) | Method and device for deeply removing sulfide in MTBE | |
| CN106699501A (en) | Method for producing elemental N-alkanes | |
| RU2714651C1 (en) | Adsorption unit for preparation of hydrocarbon gas | |
| CN204509216U (en) | Catalytically cracked gasoline extracting rectifying desulfurizer | |
| CN105733647A (en) | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas | |
| CN203333598U (en) | Processing device for modifying light hydrocarbons | |
| CN106010637B (en) | A kind of condensate desulfurization stabilising arrangement and process | |
| EP3443052A1 (en) | Separation of off gases from c3 hydrocarbons in propane dehydrogenation process | |
| CN106978226B (en) | Process and system for separating heavy hydrocarbon in natural gas by cryogenic method | |
| US2596692A (en) | Method of absorbing gases, including hydrogen sulfide | |
| NO842029L (en) | Separation of methane-rich gas, carbon dioxide and hydrogen from mixtures with light hydrocarbons | |
| CN107746366A (en) | The method that isopentane is extracted from naphtha | |
| CN207749076U (en) | A kind of refinery product's upgrading synergy and hydrogen recovery system | |
| CN103725340A (en) | Process for desulfurizing and purifying petroleum and natural gas | |
| CN108865246B (en) | Method for removing volatile sulfide in mixed hydrocarbon | |
| US2732414A (en) | fractionator | |
| CN103215066B (en) | Distillation separation device and method for liquid hydrocarbon mixture | |
| CN206751752U (en) | The system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas | |
| CN106588541B (en) | A kind of extracting torch tank lime set recycle device | |
| CN106187664B (en) | The method for preparing isobutene | |
| US2726191A (en) | Processing raw natural gas to recover gaseous and gasoline hydrocarbons |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180112 Address after: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee after: China Petroleum Engineering Construction Co Ltd Address before: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee before: Engineering Design Co., Ltd., China Petroleum Group |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20210224 Address after: 100007 No. 9 North Main Street, Dongcheng District, Beijing, Dongzhimen Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Address before: No. 6, Sichuan hi tech Zone, sublime Road, Chengdu, Sichuan Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. |