CN104449844A - Delayed coking process for coal tar - Google Patents
Delayed coking process for coal tar Download PDFInfo
- Publication number
- CN104449844A CN104449844A CN201310452685.9A CN201310452685A CN104449844A CN 104449844 A CN104449844 A CN 104449844A CN 201310452685 A CN201310452685 A CN 201310452685A CN 104449844 A CN104449844 A CN 104449844A
- Authority
- CN
- China
- Prior art keywords
- oil
- coal tar
- gas
- coking
- obtains
- 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.)
- Pending
Links
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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
Landscapes
- 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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a delayed coking process for coal tar. Coal tar enters a raw oil buffering tank after coal tar/product heat exchange, light components in coal tar enter a fractionation tower from the top of the raw oil buffering tank; heavy components in the raw oil buffering tank are conveyed in the radiation section of a heating furnace through the charge pump of the heating furnace and further heated to 350-480 DEG C, and enter a coke tower for a coking reaction under a pressure of 0.1-0.5MPa and an R value of 0.1-0.4 to generate oil gas and coke; steam is injected in the inlet of the radiation section. The oil gas generated by the reaction enters the fractionation tower for separation, so as to obtain diesel and wax oil components, the oil gas output from the top of the fractionation tower is cooled and separated to obtain gasoline and rich gas, the gasoline, diesel and wax oil components are conveyed to a downstream hydrogenation device for generating clean fuel oil, and the rich gas is used as a hydrogen production raw material or a fuel gas for the heating furnace. The process is reasonable, high in liquid yield, low in energy consumption and saving in investment compared with the prior art.
Description
Technical field
The present invention relates to the technological method belonging to tar resource Optimum utilization, relates to a kind of delay coking of coal tar technique of improvement.Specifically, relating to a kind of by improving feedstock approach and post processing mode improves coal tar processing, shortens flow process, reduces investment, energy-conservation, liquid can also be improved simultaneously and receive.
Background technology
Traditional coal tar processing delayed coking pretreatment technology adopts conventional residual oil delayed coking complete processing.
Delay coking of coal tar pretreatment technology adopts conventional residual oil complete processing, does not utilize coal tar characteristic well, carries out differential process.Major defect has: 1. due in coal tar containing easy condensation component under lesser temps, enter fractionation column base after heat exchange, easily coking in separation column, affects long-term operation; 2. with conventional slag oil phase ratio, containing more light constituent component in coal tar, part light constituent is not separated in advance, together enters process furnace, and energy consumption is high; 3. in coal tar, light constituent component is not separated in advance and together enters process furnace and coke drum, and the at high temperature generating portion cracking of part light constituent produces rich gas, and hydrogen component natively little in coal tar is reduced further, reduces liquid simultaneously and receives; 4. because coal tar ratio of carbon-hydrogen is high, in rich gas, C3, C4 component concentration is few, reclaims liquefied gas deficiency in economic performance.
Chinese patent CN1485404A is open introduces process furnace with coal tar being preheated to coalite tar in 300-380 DEG C, coke drum is entered after process furnace is heated to 480-550 DEG C, pyrogenic reaction is carried out under the pressure of 0.8-2.0Mpa, the coke generated in coke drum discharges coke drum, generation oil after coking enters extraction tower, alkaline solution is added in extraction tower, the aldehydes matter extracted goes out extraction tower, extract the fraction oil after aldehydes matter and enter separation column, isolate light hydrocarbon material, petroleum naphtha and diesel oil blending component that carbon chain lengths is less than 5 respectively.
Chinese patent CN1664068A is open enters coke drum with by coal tar after process furnace is heated to 500-520 DEG C, carries out pyrogenic reaction, through oil fuel, liquefied gas and coke that coking obtains under the pressure of 0.22-0.26Mpa.Adopt full cut delay coking process.
Chinese patent CN101429456A invention provides the combined technical method of a kind of delay coking of coal tar and hydrogenation.This invention adopts the method for delayed coking and hydrogenation to coal tar, and carry out delayed coking, hydrogenation and rear refining, hydrogenation comprises hydrotreatment, hydrofining and hydrocracking.The key of this invention utilizes delayed coking and hydrogenation combination technique technology, and the processing condition of adjustment delayed coking and hydrogenation technique, realize the final purpose of coal tar upgrading.
But the technology adopted disclosed in above-mentioned patent does not make full use of coal tar characteristic.
Summary of the invention
The object of the invention is to the deficiency overcoming above-mentioned prior art, provide a kind of and technology is utilized to coal tar processing optimization.
Compared with vacuum residuum, warm coal tar complicated components, ratio of carbon-hydrogen are high, and light constituent is high.The object of the invention makes full use of coal tar characteristic, and coal tar processing is optimized on existing Delayed Coking Technology basis.
Delay coking process provided by the invention comprises the steps:
1. first by behind coal tar and product heat exchange to 200 ~ 350 DEG C, stock oil surge tank is mixed into turning oil;
2. in the coal tar that 1. obtains of step, comparatively light constituent enters separation column from raw material surge tank top;
3. in the coal tar that 1. obtains of step, heavy constituent furnace charge is pumped into process furnace and is heated to 350 ~ 480 DEG C further, and 0.1 ~ 0.5MPa enters coke drum and carries out pyrogenic reaction, recycle ratio: 0.1 ~ 0.6, generates oil gas and coke;
4. at process furnace radiation section entrance injecting steam, improve heating furnace tube flow velocity, prevent tube coking, injecting steam amount is 1 ~ 3% of inlet amount;
5. the oil gas that the reaction that 3. obtains of step produces enters separation column and is separated, and obtains diesel oil, wax oil component send hydrogenation unit to produce oil fuel;
6. the tower top oil gas that 5. step obtains enters fractionation tower top catch pot carry out oil, gas, water separation through separation column head space cooler, water cooler cooling, and gasoline is extracted out by petrol-feed pump and sent hydrogenation unit to produce oil fuel;
7. generate oil at the bottom of the tower that 5. obtains of step after recycle pump boosting, to turn back to stock oil feeding line mix with coal tar.
As Optimization Technology technical scheme, core of the present invention is that raw material enters tower flow scheme and Conventional delayed coking process simplification.Current Conventional delayed coking raw material enters tower flow process: stock oil is delivered to diesel oil/stock oil heat exchange, the laggard separation column heat exchanging segment of wax oil/stock oil heat exchange by feedstock pump, with the deep fat gas contact heat-exchanging from top of coke tower; In stock oil, the above last running of wax oil flows at the bottom of tower together with the turning oil be condensed in deep fat gas, extracts out go coking heater to heat after filtering with furnace charge pump; At boiler tube note 3.5MPa steam, improve the stream of oil gas in boiler tube to prevent tube coking; Coke drum bottom is entered by four-way valve after process furnace material is rapidly heated; Follow-uply join rich gas compression, conventional four tower Vapor recovery unit, rich gas desulfurization, desulfuration of liquefied gas and mercaptan removal.Owing to containing easy condensation component in coal tar, if directly enter separation column after raw material heat exchange, when the high-temperature oil gas heat exchange next with coke drum, can there is condensation reaction and generate coke in the component of these easy condensations, affect device long-term operation.Directly do not enter separation column after raw material heat exchange of the present invention but generate after oil mixes with Fractionator Bottom and enter stock oil surge tank, in coal tar, comparatively light constituent enters separation column from stock oil surge tank top, mixing oil in stock oil surge tank enters process furnace, then removes separation column.Simultaneously because coal tar ratio of carbon-hydrogen is high, the rich gas productive rate produced by pyrogenic reaction is low, only have 3.5% (conventional coking 12.5%), and in rich gas, C3, C4 component is also low, only have 25% (conventional coking 38%), reclaim wherein liquefied gas cost so too high.Optimizing Flow of the present invention, does not reclaim liquefied gas, eliminates conventional four tower Vapor recovery unit, desulfuration of liquefied gas and mercaptan removal, shortens flow process, investment reduction.
Adopt the present invention to increase liquid receipts principle as follows: in coal tar, light constituent is separated from raw material surge tank, after avoiding this part cut to enter process furnace, coke drum, at high temperature cracking produces rich gas, reduces gas phase yield, increases liquid and receives.
Adopt energy-saving principle of the present invention as follows: in coal tar, light constituent is separated from raw material surge tank, furnace charge amount reduces, and effectively reduces process furnace load, energy efficient.
Accompanying drawing explanation
Fig. 1 is the schema of delay coking of coal tar technique of the present invention.
In figure, code name illustrates: 1-coal tar/product interchanger; 2-stock oil surge tank; 3-furnace charge pump; 4-process furnace; 5-coke drum; 6-circulating oil pump; 7-separation column; 8-fractionation overhead condenser; 9-separation column top knockout drum
Embodiment
As shown in Figure 1, coal tar enters stock oil surge tank 2 after coal tar-product interchanger 1 heat exchange, and in coal tar, light constituent accounts for about 20% of raw material, enters separation column 7 from stock oil surge tank 2 top; In stock oil surge tank 2, heavy constituent is sent into process furnace 4 radiation section through furnace charge pump 3 and is heated to 350 ~ 480 DEG C further, 0.1 ~ 0.5MPa, and recycle ratio enters coke drum 5 for 0.2 ~ 0.5 time and carries out pyrogenic reaction, generates oil gas and coke; At radiation section entrance injecting steam.The oil gas that reaction produces enters separation column 7 and is separated, and obtains diesel oil, wax oil component, and separation column ejects the oil gas come and obtains gasoline and rich gas through overcooling, separation.Stock oil character is in table 1, and operational condition is in table 2, and material balance table is in table 3.
Table 1 stock oil character
| Character | Unit | Stock oil |
| Proportion d 20 4 | Kg／m 3 | 1034 |
| Sulfur-bearing | m％ | 0.16 |
| Carbon residue | m％ | 5.0 |
| Ash content | m％ | 0.038 |
| Bituminous matter | m％ | 0.6 |
| Colloid | m％ | 73 |
| Stable hydrocarbon | m％ | 9 |
| Aromatic hydrocarbon | m％ | 17.4 |
Table 2 operational condition table
| Sequence number | Operational condition | Embodiment 1 | Remarks |
| 1 | Raw material surge tank temperature, DEG C | 280 | |
| 2 | Furnace outlet temperature, DEG C | 480 | |
| 3 | Coke column bottom temperature, DEG C | 472 | |
| 4 | Top of coke tower pressure, Mpa | 0.17 | |
| 5 | Top of coke tower temperature, DEG C | 420 | |
| 6 | Recycle ratio | 0.4 | |
| 7 | Water injection rate, % | 1.2 |
Table 3 material balance table
Claims (4)
1. a delay coking of coal tar technique, its feature comprises the steps:
1. first by behind coal tar and product heat exchange to 200 ~ 350 DEG C, stock oil surge tank is mixed into turning oil;
2. in the coal tar that 1. obtains of step, comparatively light constituent enters separation column from raw material surge tank top;
3. in the coal tar that 1. obtains of step, heavy constituent furnace charge is pumped into process furnace and is heated to 350 ~ 480 DEG C further, and 0.1 ~ 0.5MPa enters coke drum and carries out pyrogenic reaction, recycle ratio: 0.1 ~ 0.6, generates oil gas and coke;
4. at process furnace radiation section entrance injecting steam, improve heating furnace tube flow velocity, prevent tube coking, injecting steam amount is 1 ~ 3% of inlet amount;
5. the oil gas that the reaction that 3. obtains of step produces enters separation column and is separated, and obtains diesel oil, wax oil component send hydrogenation unit to produce oil fuel;
6. the tower top oil gas that 5. step obtains enters fractionation tower top catch pot carry out oil, gas, water separation through separation column head space cooler, water cooler cooling, and gasoline is extracted out by petrol-feed pump and sent hydrogenation unit to produce oil fuel;
7. generate oil at the bottom of the tower that 5. obtains of step after recycle pump boosting, to turn back to stock oil feeding line mix with coal tar.
2. delay coking of coal tar technique according to claim 1, after it is characterized in that coal tar and product heat exchange, does not directly enter separation column, is first separated light constituent, rear coking.
3. delay coking of coal tar technique according to claim 1 and 2, it is characterized in that furnace outlet temperature is 420 ~ 470 DEG C, top of coke tower pressure is 0.1 ~ 0.4MPa, recycle ratio: 0.2 ~ 0.5.
4. delay coking of coal tar technique according to claim 1 and 2, is characterized in that not reclaiming liquefied gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310452685.9A CN104449844A (en) | 2013-09-17 | 2013-09-17 | Delayed coking process for coal tar |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310452685.9A CN104449844A (en) | 2013-09-17 | 2013-09-17 | Delayed coking process for coal tar |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104449844A true CN104449844A (en) | 2015-03-25 |
Family
ID=52896607
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310452685.9A Pending CN104449844A (en) | 2013-09-17 | 2013-09-17 | Delayed coking process for coal tar |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104449844A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107541247A (en) * | 2017-10-04 | 2018-01-05 | 山东胜星化工有限公司 | A kind of sump oil continues uninterrupted freshening device |
| CN115138666A (en) * | 2021-03-30 | 2022-10-04 | 陕西天鼎工程技术有限公司 | Continuous treatment process for tar residues |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4797195A (en) * | 1988-02-26 | 1989-01-10 | Amoco Corporation | Three zone hydrocracking process |
| CN101256400A (en) * | 2008-04-09 | 2008-09-03 | 清华大学 | Control method for delay coking stove |
| CN101538482A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Medium and low temperature coal tar deep processing method |
| CN102876376A (en) * | 2012-09-27 | 2013-01-16 | 大连理工大学 | Method for improving hydrogenation production of gasoline and diesel oil by coal tar |
-
2013
- 2013-09-17 CN CN201310452685.9A patent/CN104449844A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4797195A (en) * | 1988-02-26 | 1989-01-10 | Amoco Corporation | Three zone hydrocracking process |
| CN101256400A (en) * | 2008-04-09 | 2008-09-03 | 清华大学 | Control method for delay coking stove |
| CN101538482A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Medium and low temperature coal tar deep processing method |
| CN102876376A (en) * | 2012-09-27 | 2013-01-16 | 大连理工大学 | Method for improving hydrogenation production of gasoline and diesel oil by coal tar |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107541247A (en) * | 2017-10-04 | 2018-01-05 | 山东胜星化工有限公司 | A kind of sump oil continues uninterrupted freshening device |
| CN115138666A (en) * | 2021-03-30 | 2022-10-04 | 陕西天鼎工程技术有限公司 | Continuous treatment process for tar residues |
| CN115138666B (en) * | 2021-03-30 | 2024-06-04 | 陕西天鼎工程技术有限公司 | Continuous treatment process for tar residues |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101597518A (en) | A kind of improved delay coking process | |
| CN104673371B (en) | A kind of method for improving delayed coking liquid product yield | |
| CN104030381B (en) | A kind of system and method utilizing oil field ground waste heat to prepare injection boiler feedwater | |
| CN101591561A (en) | A kind of delay coking process | |
| CN102786986A (en) | Refining technology of microalgae pyrolysis oil | |
| CN104987885B (en) | A kind of Fischer-Tropsch synthesis oil and coal tar are hydrogenated with the technique and device of production national standard oil altogether | |
| CN102220165A (en) | Process for delaying coking | |
| CN105647581A (en) | Catalytic gasoline hydrogenation method | |
| CN104449844A (en) | Delayed coking process for coal tar | |
| CN104086346B (en) | A kind of energy reclaiming method of oxygenatedchemicals propylene technique | |
| CN105713647B (en) | A kind of utilization coal tar maximization prepares the method and device of carbolic oil and diesel oil | |
| CN102161900A (en) | Device and method for extracting oil from blocky oil shale with high efficiency | |
| CN104673372A (en) | Method for improving distribution of delayed coking product | |
| CN102220166A (en) | Delayed coking method | |
| CN101962565B (en) | Quench oil viscosity reducing process for two quench oil systems | |
| CN103215062A (en) | Delay coking processing method of inferior residual oil | |
| CN104449843A (en) | Step-by-step cracking and hydrogen-present coking process for coal tar | |
| CN103361112B (en) | Device for blending catalytic slurry oil in delayed coking technology and method thereof | |
| CN101948698A (en) | Novel energy-saving device for condensing and recovering oil shale in retorting oil gas and method | |
| CN109652121B (en) | Undoped full-fraction ethylene tar delay coking equipment | |
| CN102443408B (en) | Pressure reduction distillation process method | |
| CN204824751U (en) | Ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether | |
| CN204848770U (en) | Reduce low recycle ratio coker of coke yield | |
| CN105567294B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN220724051U (en) | Petroleum atmospheric and vacuum distillation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB02 | Change of applicant information |
Address after: Hangzhou road in Baohe District of Hefei city in Anhui province 230091 and Tibet road junction of the northeast corner of the Binhu Times Square building C3 No. 1301 Applicant after: ANHUI SHIHUA ENGINEERING & TECHNOLOGY CO., LTD. Address before: 246002 No. 8, No. 1, oil production road, Anqing, Anhui Applicant before: ANHUI SHIHUA ENGINEERING & TECHNOLOGY CO., LTD. |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 246002 ANQING, ANHUI PROVINCE TO: 230091 HEFEI, ANHUI PROVINCE |
|
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150325 |