CN1038043C - Thermal cracking of a hydrocarbon feed - Google Patents
Thermal cracking of a hydrocarbon feed Download PDFInfo
- Publication number
- CN1038043C CN1038043C CN94191543A CN94191543A CN1038043C CN 1038043 C CN1038043 C CN 1038043C CN 94191543 A CN94191543 A CN 94191543A CN 94191543 A CN94191543 A CN 94191543A CN 1038043 C CN1038043 C CN 1038043C
- Authority
- CN
- China
- Prior art keywords
- heavy product
- product stream
- product flow
- reaction chamber
- vertical tube
- 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.)
- Expired - Fee Related
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/06—Vacuum distillation
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Processing Of Solid Wastes (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
烃原料的热解方法包括：在加热炉(1)中加热原料；向反应室(15)提供原料；把来自反应室(15)的物流分离为轻产品流和重产品流；向真空蒸馏塔(30)提供重产品流以使重产品流分离为不同馏分，其中，向真空蒸馏塔中提供重产品流包括：重产品流通过流量控制阀(36)，向上通过竖管(38)，竖管的长度使竖管(38)末端处流体压力能抑制竖管下端处的汽化，重产品流再经输送管(40)流入真空蒸馏塔(30)，输送管(40)的结构应使其出口处流体压力与真空蒸馏塔(30)中流体压力相等。
The pyrolysis method of hydrocarbon raw material comprises: heating raw material in heating furnace (1); Supply raw material to reaction chamber (15); Separate the stream from reaction chamber (15) into light product stream and heavy product stream; (30) Provide the heavy product stream to separate the heavy product stream into different fractions, wherein, providing the heavy product stream to the vacuum distillation column includes: the heavy product stream passes through the flow control valve (36), passes upwardly through the vertical pipe (38), vertically The length of the pipe makes the fluid pressure at the end of the standpipe (38) suppress the vaporization at the lower end of the standpipe, and the heavy product stream flows into the vacuum distillation tower (30) through the delivery pipe (40). The structure of the delivery pipe (40) should make it The fluid pressure at the outlet is equal to the fluid pressure in the vacuum distillation tower (30).
Description
The present invention relates to as the oil handbook sixth version, Elsevier, 1983, the pyrolysis of the hydrocarbon feed described in the 279-281 page or leaf.
The pyrolytic process of hydrocarbon feed comprises: heating raw under the temperature range of the pressure range 0.2 to 5Mpa and 390 to 530 ℃; Raw material is sent into reaction chamber; Logistics from reaction chamber is separated into light product stream and heavy product flow; To weigh product flow and send into vacuum tower, so that heavy product flow is separated into different fractions under the temperature range of 1 to 10kpa pressure range and 320 to 400 ℃.
In currently known methods, use pipeline that heavy product flow is delivered to vacuum tower, because the pressure of heavy product flow is higher than the pressure in the vacuum tower, should equal pressure reduction between heavy product flow and vacuum tower along the pressure drop of pipeline.A kind of method that realizes this quite high pressure drop along pipeline is to provide a restriction to pipeline, for example with the form of flowrate control valve.Yet, when heavy product flow during by throttling, vaporization fast takes place on flowrate control valve.This quick vaporization is accompanied by the formation of very little drop, is difficult for handling in vacuum tower.
The invention provides a kind of simple method that suppresses to vaporize on the restriction.
For achieving the above object, hydrocarbon feed pyrolytic process according to the present invention comprises: heating raw under the temperature range of the pressure range 0.2 to 5Mpa and 390 to 530 ℃; Raw material is sent into reaction chamber; Logistics from reaction chamber is separated into light product stream and heavy product flow; To weigh product flow and send into vacuum tower, so that heavy product flow is separated into different fractions under the temperature range of 1 to 10kpa pressure range and 320 to 400 ℃, wherein, provide heavy product flow to comprise to vacuum tower: heavily restriction is crossed in products in circulation, upwards through vertical tube, the length of vertical tube should make vertical tube end fluid pressure energy suppress the vaporization of vertical tube lower end, heavy product flow then flows into vacuum tower through transfer lime, and the structure of transfer lime should make its exit hydrodynamicpressure equate with hydrodynamicpressure in the vacuum tower.
Word in specification sheets and claims " structure of transfer lime " be used to refer to transfer lime help to produce characteristics along the pressure drop of transfer lime, resemble size and the bend pipe in other flow resistance such as the transfer lime or the turnover of U type of transfer lime.
By example the present invention is described in more detail referring now to accompanying drawing, wherein,
Accompanying drawing 1 is the schematic flow sheet of the method according to this invention.
Accompanying drawing 2 is another kind of schematic flow sheets of the method according to this invention.
About accompanying drawing 1.The flow process of the method according to this invention comprises process furnace 1 that has roasting kiln 2 and chimney 3 and the heating tube 4 that places process furnace 1.Heating tube 4 is connected on inlet tube 7 and the outlet pipe 9.
The length of vertical tube 38 is decisions like this, in normal running, makes vertical tube 38 lower end fluid pressure energies suppress the vaporization of vertical tube lower end fluidic.In specification sheets and claims, use " vaporization of suppression fluid " words and phrases to be meant small volume of fluid vaporization (being lower than about 5% (volume)) is arranged at the most.
The structure of transfer lime 40 is like this decisions, and under normal operation, the hydrodynamicpressure of transfer lime 40 exit end 41 equates with hydrodynamicpressure in the vacuum tower 30.This means that the design of transfer lime 40 makes the suffered friction of fluid of flowing through transfer lime 40 equal the pressure reduction of 30 of the exit of vertical tube 38 and vacuum towers.In the case, transfer lime 40 comprises some straight tubes 43 that the crooked pipe connecting in order to the form of U type pipe connecting 44 is connected.
In the normal running, providing continuously 3000 tons/day hydrocarbon feed under the pressure of 3Mpa in process furnace 1, hydrocarbon feed heats under 450 ℃ the temperature in process furnace 1.Then, the hydrocarbon feed of heating is sent into reaction chamber 15, hydrocarbon feed is in this cracking.In cyclonic separator 20, be separated into from exporting 21 900 tons/day light products that shift out and from the product flow of reaction chamber 15 from exporting 24 2100 tons/day heavy products that shift out, provide heavy product by piping 26 to the vacuum tower of under 5kpa pressure and 380 ℃ of temperature, operating 30, in vacuum tower 30, heavy product flow is separated into 200 tons/day the gaseous fraction that shifts out from outlet pipe 31,400 tons/day the middle runnings of shifting out from outlet pipe 33,1500 tons/day the resistates that shifts out from resistates outlet pipe 32.
Pressure drop on the flowrate control valve 36 is 150KPa.
The length of vertical tube 38 is 15n, and there is the fluidic vaporization that has prevented at the dirty end place of flowrate control valve 36 in fluidic in the vertical tube 38.
The length of transfer lime 40 is 70m, and the mean inside diameter of transfer lime 40 is 50cm, and transfer lime comprises 4 U type pipe connectings.The ingress hydrodynamicpressure of transfer lime 40 is 60kpa, and the exit hydrodynamicpressure equates with hydrodynamicpressure in the vacuum tower 30.
Save vertical tube 38 and will cause in flowrate control valve 36 places or near the vaporization it, this vaporization is uncontrolled and is accompanied by the formation of minimum drop.
Relate to accompanying drawing 2 now, another flow process of sending fully of its expression the method according to this invention.The part similar with the flow process described in the accompanying drawing 1 has identical reference number.
In the flow process of accompanying drawing 2, in distillation tower 50, be separated into from exporting the 51 light products streams that shift out and from exporting the 52 heavy product flow that shift out from the logistics of reaction chamber 15.
Then, provide heavy product flow by piping 26 to vacuum tower 30.Suitable backflow is provided and provides the equipment of stripping medium not express to distillation tower 50 tops to distillation tower 50 bottoms.
Crooked pipe connecting 44 can have the U type shown in attached Fig. 1 and 2, perhaps has the L type.
There is the fluidic vaporization that has prevented at the dirty end of restriction place in fluidic in the vertical tube.Save vertical tube and will cause at the restriction place or near the vaporization it, this vaporization is uncontrolled and is accompanied by the formation of very little drop.In vacuum tower, this this fine droplet can not be separated from air-flow, so that drop carried secretly out by the cut that leaves vacuum tower from middle cut outlet pipe, is perhaps left the air-flow of vacuum distilling top of tower from outlet pipe and carries secretly out.This separation efficiency of carrying secretly vacuum tower produces adverse influence.
As the described vertical tube 38 of attached Fig. 1 and 2 are standpipes, and certainly, this vertical tube also can be an inclined tube, as long as there are enough fluids to prevent devaporation in normal running in the vertical tube.
Claims (4)
1. the method for pyrolysis of hydrocarbon feed comprises: heating raw under the temperature range of the pressure range 0.2 to 5Mpa and 390 to 530 ℃; Supply raw materials to reaction chamber; Logistics from reaction chamber is separated into light product stream and heavy product flow; Provide heavy product flow so that be separated into different fractions under the temperature range of heavy product flow 1 to 10kpa pressure range and 320 to 400 ℃ to vacuum tower, wherein, provide heavy product flow to comprise to vacuum tower: heavily restriction is crossed in products in circulation, upwards flow through vertical tube, the length of vertical tube makes vertical tube end fluid pressure energy suppress the vaporization of vertical tube lower end, heavy product flow flows into vacuum tower through transfer lime again, and the structure of transfer lime should make its exit hydrodynamicpressure equate with hydrodynamicpressure in the vacuum tower.
2. according to the process of claim 1 wherein, transfer lime comprises many straight lengths that connected by crooked pipe connecting.
3. according to the method for claim 1 or 2, wherein, in cyclonic separator, be separated into light product stream and heavy product flow from the logistics of reaction chamber.
4. according to the method for claim 1 or 2, wherein, in distillation tower, be separated into light product stream and heavy product flow from the logistics of reaction chamber.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP93200832 | 1993-03-22 | ||
| EP93200832.9 | 1993-03-22 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1119875A CN1119875A (en) | 1996-04-03 |
| CN1038043C true CN1038043C (en) | 1998-04-15 |
Family
ID=8213718
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN94191543A Expired - Fee Related CN1038043C (en) | 1993-03-22 | 1994-03-18 | Thermal cracking of a hydrocarbon feed |
Country Status (17)
| Country | Link |
|---|---|
| EP (1) | EP0690900B1 (en) |
| JP (1) | JP3499873B2 (en) |
| KR (1) | KR100295069B1 (en) |
| CN (1) | CN1038043C (en) |
| AU (1) | AU675530B2 (en) |
| CA (1) | CA2158765C (en) |
| CZ (1) | CZ283755B6 (en) |
| DE (1) | DE69400917T2 (en) |
| ES (1) | ES2096463T3 (en) |
| FI (1) | FI119938B (en) |
| HU (1) | HU216102B (en) |
| MD (1) | MD1207C2 (en) |
| NO (1) | NO309388B1 (en) |
| RU (1) | RU2114894C1 (en) |
| SA (1) | SA94140602B1 (en) |
| WO (1) | WO1994021749A1 (en) |
| ZA (1) | ZA941922B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR960031577A (en) * | 1995-02-03 | 1996-09-17 | 신호근 | High vacuum refinery and method |
| KR20020051940A (en) * | 1999-12-10 | 2002-06-29 | 시게히사 요시히로 | Petroleum processing method and device therefor |
| RU2372374C1 (en) * | 2008-04-22 | 2009-11-10 | Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") | Processing method of black oil fuel and installation for its implementation |
| WO2014124517A1 (en) | 2013-02-15 | 2014-08-21 | Rival Technologies Inc. | Method of upgrading heavy crude oil |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3025232A (en) * | 1957-07-12 | 1962-03-13 | Texaco Inc | Automatic control of the viscosity of a fractionator product |
| US3075578A (en) * | 1959-07-27 | 1963-01-29 | Sumiya Shinzo | Multiple vacuum effect evaporator |
| US5110447A (en) * | 1988-09-12 | 1992-05-05 | Kasten, Eadie Technology Ltd. | Process and apparatus for partial upgrading of a heavy oil feedstock |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2493171A1 (en) * | 1980-11-06 | 1982-05-07 | Bailet Victor | Vacuum distn. using thermal siphon to separate vessels - eliminates use of extn. pumps for removing product or bottoms |
-
1994
- 1994-03-18 RU RU95121591A patent/RU2114894C1/en active
- 1994-03-18 JP JP52066494A patent/JP3499873B2/en not_active Expired - Fee Related
- 1994-03-18 CZ CZ952440A patent/CZ283755B6/en not_active IP Right Cessation
- 1994-03-18 AU AU65038/94A patent/AU675530B2/en not_active Ceased
- 1994-03-18 HU HUP9502609A patent/HU216102B/en not_active IP Right Cessation
- 1994-03-18 ES ES94912498T patent/ES2096463T3/en not_active Expired - Lifetime
- 1994-03-18 MD MD96-0308A patent/MD1207C2/en not_active IP Right Cessation
- 1994-03-18 ZA ZA941922A patent/ZA941922B/en unknown
- 1994-03-18 WO PCT/EP1994/000895 patent/WO1994021749A1/en not_active Ceased
- 1994-03-18 KR KR1019950704030A patent/KR100295069B1/en not_active Expired - Fee Related
- 1994-03-18 DE DE69400917T patent/DE69400917T2/en not_active Expired - Lifetime
- 1994-03-18 EP EP94912498A patent/EP0690900B1/en not_active Expired - Lifetime
- 1994-03-18 CA CA002158765A patent/CA2158765C/en not_active Expired - Fee Related
- 1994-03-18 CN CN94191543A patent/CN1038043C/en not_active Expired - Fee Related
- 1994-03-22 SA SA94140602A patent/SA94140602B1/en unknown
-
1995
- 1995-09-20 FI FI954441A patent/FI119938B/en active IP Right Grant
- 1995-09-20 NO NO953715A patent/NO309388B1/en not_active IP Right Cessation
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3025232A (en) * | 1957-07-12 | 1962-03-13 | Texaco Inc | Automatic control of the viscosity of a fractionator product |
| US3075578A (en) * | 1959-07-27 | 1963-01-29 | Sumiya Shinzo | Multiple vacuum effect evaporator |
| US5110447A (en) * | 1988-09-12 | 1992-05-05 | Kasten, Eadie Technology Ltd. | Process and apparatus for partial upgrading of a heavy oil feedstock |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0690900A1 (en) | 1996-01-10 |
| DE69400917D1 (en) | 1996-12-19 |
| ES2096463T3 (en) | 1997-03-01 |
| WO1994021749A1 (en) | 1994-09-29 |
| MD1207B2 (en) | 1999-04-30 |
| CZ283755B6 (en) | 1998-06-17 |
| CN1119875A (en) | 1996-04-03 |
| EP0690900B1 (en) | 1996-11-13 |
| NO953715D0 (en) | 1995-09-20 |
| DE69400917T2 (en) | 1997-05-22 |
| FI119938B (en) | 2009-05-15 |
| HU216102B (en) | 1999-04-28 |
| HUT73408A (en) | 1996-07-29 |
| JPH08511039A (en) | 1996-11-19 |
| FI954441A7 (en) | 1995-09-20 |
| RU2114894C1 (en) | 1998-07-10 |
| NO309388B1 (en) | 2001-01-22 |
| HU9502609D0 (en) | 1995-11-28 |
| CA2158765C (en) | 2004-03-30 |
| NO953715L (en) | 1995-09-20 |
| CZ244095A3 (en) | 1996-01-17 |
| MD960308A (en) | 1997-10-31 |
| ZA941922B (en) | 1994-10-14 |
| CA2158765A1 (en) | 1994-09-29 |
| MD1207C2 (en) | 1999-11-30 |
| JP3499873B2 (en) | 2004-02-23 |
| KR960701171A (en) | 1996-02-24 |
| SA94140602B1 (en) | 2005-07-31 |
| KR100295069B1 (en) | 2001-10-24 |
| AU6503894A (en) | 1994-10-11 |
| FI954441A0 (en) | 1995-09-20 |
| AU675530B2 (en) | 1997-02-06 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 19980415 Termination date: 20120318 |