CN104312622A - Processing method for heavy oil - Google Patents
Processing method for heavy oil Download PDFInfo
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- CN104312622A CN104312622A CN201410627413.2A CN201410627413A CN104312622A CN 104312622 A CN104312622 A CN 104312622A CN 201410627413 A CN201410627413 A CN 201410627413A CN 104312622 A CN104312622 A CN 104312622A
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- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a processing method for heavy oil. A gas-solid separating zone is formed in the upper part of a reactor, a thermal cracking zone is formed in the middle part, a gasifying zone is formed in the lower part, raw materials are led into the reactor from the bottom part of the gas-solid separating zone and are dispersed into oil drops through an atomizer, the light components in the oil drops are volatilized into oil gas in the process that the oil drops fall down in the thermal cracking zone, and the heavy components are condensed into tar. Therefore, the processing method has obvious social benefit and economic benefit.
Description
Technical field
The present invention relates to a kind of working method of heavy oil.
Background technology
Along with the progress of science and technology and the development of economic construction; the problem of energy dilemma has become the matter of utmost importance hindering world's every country Economic development and construction; by the impact of resource; crude oil in China disparities between supply and demand become increasingly conspicuous; from 1993; China becomes net import of oil state, needs every year to spend a large amount of foreign exchange Imported oils and petroleum products.
In China's major part crude oil, residue content is high, and lightweight oil content is low, and some mink cell focuses (viscous crude) output constantly increases and the introduction of the external heavy crude of part makes heavy oil lighting problem more outstanding in recent years in addition.Heavy oil upgrading method often has the methods such as catalytic cracking, solvent deasphalting, visbreaking, coking, thermally splitting, heavy-oil hydrogenation, generally speaking, nothing more than hydrogenation and the large class of decarburization two, wherein heavy oil decarburization processing is the major way of current refining of petroleum, and the Appropriate application deviating from carbon is solved always very well.Heavy oil catalytic pyrolysis, flexicoking, fluid coking, heavy oil fluidized upgrading etc. are mainly contained in heavy oil solid phase carrier circulation cracking technology.
In face of the market competition of fierceness, the method for Technological Economy excellence can bring beyond thought profit.Change the Main Means that cracking (FCC) was once or in the future certain areas processing heavy oil, but the problems such as along with mixing the raising of refining ratio, FCC apparatus heat surplus, device coking are serious, regenerated flue gas contaminate environment become increasingly conspicuous.So hot-work recently and coking process are had an optimistic view of by everybody once again.
Heat processing technique can produce liquid product to greatest extent, especially diesel oil distillate.One of hot-work form coking principal mode has autoclave, open hearth, delay, contact, fluidisation and flexicoking etc. 6 kinds.Two kinds of technique is due to backward in technique, batch production, the shortcoming such as labor condition is poor, consumption steel are many and floor space is large above, is eliminated.Contact coking technique because flow process and equipment are complicated, investment and maintenance cost high and develop less.Though fluid coking developed to some extent in the fifties, because the fluid coke purposes of by-product is extensive not as delay coke, so this technology popularization obtains unhappy.
The product of coking can be divided into two classes: a class is product liquid and gaseous product, another kind of, is coke.Refinery coke is broad-spectrum a kind of product, but along with the development of coking industry, surplus will appear in refinery coke product.On the other hand, poor quality, mink cell focus are in liberal supply, and the coke that this oil produces is difficult to find buyer's market.Flexicoking technique adopts fluid coking technology to process this inferior feedstock oil, and the coke formed is transported to vapourizing furnace and produces synthesis gas.
Flexicoking and fluid coking temperature of reaction low about 350 DEG C-600 DEG C, mainly produce coker gasoline, diesel oil and the wax tailings as fcc raw material, char combustion component loops produces synthetic gas as thermal barrier, partial gasification, but pyrolysis time is long, and yield of light oil is lower; Heavy oil fluidized upgrading (as the ART technique of Engelhardt moral exploitation, the HCC technique etc. of Luoyang Petrochemical designing institute) adopts the circulating fluidized bed technique similar to heavy oil catalytic cracking process, temperature of reaction about 400 DEG C-600 DEG C, pyrolysis time is short, and yield of light oil is higher.
On the basis of fluid coking technology, the flexicoking further developed is that coke that coking is generated and air and water vapour react and forms low-calorie water-gas, as byproduct carrying device, and the therefore coke of a this flexicoker production minute quantity.Flexicoking is applicable to the heavy oil residue processing high-sulfur, high nitrogen and high metal content, and liquid is received higher.Because the investment of fluid coking and flexicoking and process cost are all far above delayed coking, thus develop very slow.The features such as delayed coking is simple, easy to operate due to technique, the handiness of device is large, and the high and on-stream time of working rate is long, development is very fast.
Heavy oil catalytic pyrolysis is except the object product obtained (petrol and diesel oil and alkene industrial chemicals), the carbon residue removed combustion heat release in a regenerator, part heatable catalyst is as the thermal source of cracking, part heat collector heat-obtaining produces steam and sends outside or generate electricity, temperature of reaction is lower about 500 DEG C-650 DEG C, higher to heavy oil ingredient requirement, do not reach fully effectively utilizing petroleum resources.
Summary of the invention
In order to solve the problems of the technologies described above, a kind of working method of heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 400 DEG C-600 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 600 DEG C-700 DEG C heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
The beneficial effect of method provided by the invention is:
Achieve inside reactor and divide desulfurization, simplify scavenging process; With Wingdale or white clouds masonry thermal barrier, make use of calcium oxide and CO 2 thermopositive reaction, reduce the recycle ratio of solid-phase thermal carrier; Institute's production of synthetic gas composition is the same with the water-gas of hard coal intermittent gasification, is conducive to the requirement that green fuel dimethyl ether is produced the most; Petroleum resources obtain fully effectively utilizing, and achieve heavy oil and process without scorification.
The advantage of reactor provided by the invention is:
The hot gas flow that reactor bottom gasification is formed to regulate after temperature with top by the droplets contact heat exchange disperseing to fall through heat exchange, the thermal source of heat scission reaction is provided, the coke that heat scission reaction generates simultaneously is all vaporized, and gasification efficiency is high, heat energy utilization is reasonable, decreases energy consumption.The heat scission reaction of stock oil and the gasification reaction of coke are integrated in a reactor and carry out, save facility investment.
Thermal cracking processes and gasification are arranged in a reactor, heavy raw oil are converted into hydrogen, dry gas, liquefied gas, gasoline and diesel oil, utilize the Mass and heat transfer advantage of adverse current bed.
Embodiment
Embodiment 1
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 560 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 700 DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Embodiment 2
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 500 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 700 DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Embodiment 3
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 410 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 615 DEG C of DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Embodiment 4
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 600 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 620 DEG C of DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Embodiment 5
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 600 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 600 DEG C of DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Embodiment 6
A working method for heavy oil, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 600 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 700 DEG C of heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Claims (1)
1. a working method for heavy oil, is characterized in that, its reactor is divided into three parts, and first part is gas solid separation district, is positioned at top; Second section is thermo-cracking district, is positioned at middle portion; Part III is vaporizing zone, is positioned at reactor lower part, and raw material introduces reactor by bottom first part, is separated into drop through spraying gun, and comparatively light constituent volatilization is for oily vapour in second section dropping process for drop, and heavy component condensation forms coke; With high-efficiency atomizing nozzle, the heavy oil being preheating to 400 DEG C-600 DEG C is sprayed into the middle part of riser tube from the opening for feed of descending riser tube, mist of oil is by 600 DEG C-700 DEG C heating of high temperature solid-state thermal barrier, vaporization and cracking falling from gasifying fluidized bed; High-temperature flue gas enters flue gas heat-exchange unit heat exchange and produces superheated vapour for gasification; Gas solid separation is carried out in the bottom that oil gas and solid-phase thermal carrier run down to riser tube; A remaining fine coke particles part falls into ash bucket, and form lime-ash, isolated gas phase outflow reactor, enters subsequent separation system and be separated into synthetic gas, liquefied gas, gasoline, diesel oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410627413.2A CN104312622A (en) | 2014-11-10 | 2014-11-10 | Processing method for heavy oil |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410627413.2A CN104312622A (en) | 2014-11-10 | 2014-11-10 | Processing method for heavy oil |
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| CN104312622A true CN104312622A (en) | 2015-01-28 |
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| CN201410627413.2A Pending CN104312622A (en) | 2014-11-10 | 2014-11-10 | Processing method for heavy oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108946741A (en) * | 2017-05-17 | 2018-12-07 | 新特能源股份有限公司 | The recovery process method of siliceous high-boiling components in polysilicon cold hydrogenation process and cold hydrogenation process |
| WO2019149008A1 (en) * | 2018-01-30 | 2019-08-08 | 浙江工业大学 | Novel high-temperature pyrolysis reaction device |
Citations (4)
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| CN1600831A (en) * | 2003-09-25 | 2005-03-30 | 田原宇 | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique |
| CN101451073A (en) * | 2007-12-06 | 2009-06-10 | 中国石油化工股份有限公司 | Method for combination processing heavy oil by pyrolysis and gasification |
| US20130206642A1 (en) * | 2011-05-31 | 2013-08-15 | China University Of Petroleum-Beijing | Integrated process for upgrading heavy oil |
| CN103773448A (en) * | 2012-10-18 | 2014-05-07 | 中国石油化工股份有限公司 | Contact cracking method and apparatus for heavy oil |
-
2014
- 2014-11-10 CN CN201410627413.2A patent/CN104312622A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1600831A (en) * | 2003-09-25 | 2005-03-30 | 田原宇 | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique |
| CN101451073A (en) * | 2007-12-06 | 2009-06-10 | 中国石油化工股份有限公司 | Method for combination processing heavy oil by pyrolysis and gasification |
| US20130206642A1 (en) * | 2011-05-31 | 2013-08-15 | China University Of Petroleum-Beijing | Integrated process for upgrading heavy oil |
| CN103773448A (en) * | 2012-10-18 | 2014-05-07 | 中国石油化工股份有限公司 | Contact cracking method and apparatus for heavy oil |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108946741A (en) * | 2017-05-17 | 2018-12-07 | 新特能源股份有限公司 | The recovery process method of siliceous high-boiling components in polysilicon cold hydrogenation process and cold hydrogenation process |
| CN108946741B (en) * | 2017-05-17 | 2020-05-12 | 新特能源股份有限公司 | Process method for recovering silicon-containing high-boiling-point substance in polycrystalline silicon cold hydrogenation process and cold hydrogenation process |
| WO2019149008A1 (en) * | 2018-01-30 | 2019-08-08 | 浙江工业大学 | Novel high-temperature pyrolysis reaction device |
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Application publication date: 20150128 |
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