CN1396236A - Delay coking process able to flexibly regulate recirculating ratio - Google Patents
Delay coking process able to flexibly regulate recirculating ratio Download PDFInfo
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- CN1396236A CN1396236A CN 02139312 CN02139312A CN1396236A CN 1396236 A CN1396236 A CN 1396236A CN 02139312 CN02139312 CN 02139312 CN 02139312 A CN02139312 A CN 02139312A CN 1396236 A CN1396236 A CN 1396236A
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- Prior art keywords
- coking
- oil
- distillation column
- fractional distillation
- raw material
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- Granted
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- 238000004939 coking Methods 0.000 title claims abstract description 107
- 238000000034 method Methods 0.000 title claims abstract description 42
- 230000003134 recirculating effect Effects 0.000 title 1
- 239000002994 raw material Substances 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 238000004508 fractional distillation Methods 0.000 claims description 22
- 239000000571 coke Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000006482 condensation reaction Methods 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims 1
- 239000003921 oil Substances 0.000 abstract description 51
- 239000007788 liquid Substances 0.000 abstract description 4
- 239000010724 circulating oil Substances 0.000 abstract description 2
- 238000005194 fractionation Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 17
- 239000000047 product Substances 0.000 description 10
- 230000003111 delayed effect Effects 0.000 description 7
- 238000000926 separation method Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 230000005855 radiation Effects 0.000 description 4
- 239000000446 fuel Substances 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
A delay coking process able to flexible regulate the circualting ratio operation features that part of the circulating oil in reaction oil vapour of coking tower is separated out by the coking fractionation tower and then proportionally mixed with the raw material of coking tower. Its advantages are flexible regulation, high total liquid output, and high quality of coker wax oil.
Description
Technical field:
The invention belongs to the refining of petroleum field, but the delay coking process of particularly a kind of flexible recycle ratio operation.
Background technology:
Delayed coking unit is a kind of degree of depth on-catalytic cracked thermocracking process, with heavy oil conversion is dry gas, liquefied petroleum gas (LPG), coker gasoline, coker gas oil, wax tailings, the heavy wax oil returns coke drum as turning oil and further carries out cracking, recycle ratio is an important operation parameter of delayed coking unit, the change of recycle ratio is to the product yield of coker, and the quality product influence is bigger.
Delayed coking unit is regulated the old process of recycle ratio, adopts reaction oil gas and coking raw material in the direct heat exchange of separation column feed zone, controls the condensation number of heavy constituent in the charging oil gas by throat-fed about regulating, thereby realizes the adjusting of recycle ratio.At present, national coker almost all adopts old process.But, when this flow process is operated than (being lower than 0.2) at partial circulating, because last opening for feed inlet amount reduces, a large amount of high-temperature oil gas directly contacts with a spot of feed oil, cause feed oil in the easy coking of separation column charging heat exchanging segment, a large amount of coke powders influence the normal operation of radiation fresh feed pump, and cause the radiating furnace tube coking and shorten the device cycle of operation.Because the feed zone linear gas velocity is higher, feed oil directly contacts with reaction oil gas, forms entrainment easily, causes wax tailings second-rate simultaneously.Production practice show, when recycle ratio less than 0.2 the time, old process is difficult to normal running.
In order to reduce coking heater load and plant energy consumption, increase device working ability significantly and to improve liquid and receive, CN 1290736A discloses a kind of with all extractions of wax slop (turning oil), enter coking heater after the coking raw material heat exchange, do not contain turning oil in the coking heater charging, this technology is not carried out the adjusting of recycle ratio, is actually a kind of one way coking process.
Increase the intermediate oil yield simultaneously in order to improve liquid yield, reduce coke yield, CN1297984A discloses and has a kind ofly combined delayed coking and solvent deasphalting are refining, improve the residual oil thermal processing method of liquid product yield, its flow process characteristics are that whole extraction the out of wax slop (turning oil) that quality is the poorest enters the solvent deasphalting unit processing, and the turning oil of coker is 330-420 ℃ coking light wax oil.This is a kind of process integration, though the adjusting of recycle ratio is more convenient, flow process is longer.
Summary of the invention:
The objective of the invention is that the wax tailings that exists at present coking process flow process is of poor quality, partial circulating is than problems such as following separation column cokings, but develop a kind of technical process of flexible recycle ratio, overcome the defective of existing delayed coking flow process, provide a kind of flexible operation, the safe delay coking process flow process that reliably can satisfy the long period production requirement to production.
But the delay coking process of a kind of flexible recycle ratio operation of the present invention, its technical scheme that adopts is as follows:
Coking raw material and following coking recycle oil are mixed into coking heater, after being heated to coking temperature, enter coke drum and carry out thermally splitting and condensation reaction, reaction oil gas advances coking fractional distillation column, the coking fractional distillation column bottom is extracted turning oil out, turning oil is after the heat exchange cooling, and a part is returned the coking fractional distillation column bottom as backflow, and a part is mixed with above-mentioned coking raw material as coking recycle oil or/and a part goes out device as product.
In the technology of the present invention, coking raw material does not advance coking fractional distillation column and contacts with pyroreaction oil gas, and recycle ratio is controlled by the coking recycle oil amount of calling in coking raw material.For example, when recycle ratio was 0, the coking recycle oil amount of calling in coking raw material was 0, this moment turning oil can get a part go out device as product.Technology of the present invention can be regulated the ratio of turning oil in each road according to different operating modes, regulates flexibility and reliability.
Coking recycle oil of the present invention can mix with coking raw material through behind the filter elimination coke powder again, can further reduce the coke powder amount that coking recycle oil carries like this, and the coking that reduces in the coking heater boiler tube takes place.
Mixing of coking recycle oil of the present invention and coking raw material can be at the coking raw material motion device to entering any one position on pipeline between the coking heater or the equipment.As required, can adopt mixing equipment to reach well-mixed purpose.
The feeding temperature of coking heater of the present invention is recommended to be controlled at 200-350 ℃.The coking heater charging comprises coking raw material and coking recycle oil, can carry out heat exchange with the medium of different potential temperatures in the device, the design of its heat exchange process and be optimized for ordinary skill in this area.
The turning oil recommended hour two tunnel that the present invention refluxes returns coking fractional distillation column, and one the tunnel returns heat exchange baffle plate top in the coking fractional distillation column, and coking fractional distillation column bottom liquid phase is returned on another road.Like this, the turning oil and the pyroreaction oil gas that return heat exchange baffle plate top in the coking fractional distillation column on the one hand carry out contact heat-exchanging on the heat exchange baffle plate, can control vapor phase temperature under the wax oil oil header easily by the heat exchange degree of depth outside coking fractional distillation column, finally reach the extraction amount of Control Circulation oil.On the other hand, return the turning oil may command coking fractional distillation column column bottom temperature of bottom liquid phase in the coking fractional distillation column.
The present invention can as surge tank, realize the control to device charging stability by establish the charging buffer device before coking heater.
The present invention compared with prior art has following unusual effect:
Can regulate the recycle ratio that the coking recycle oil amount is come the flexible device easily, recycle ratio can be between 0～1.0 flexible.The adjusting of particularly ultralow recycle ratio (being lower than 0.2) is very easy to realize, and then has improved total liquid receipts of device.
Because coking raw material does not advance separation column and reaction oil gas direct heat exchange, therefore can reduce the coking of separation column bottom, and can improve the wax oil quality.
The present invention compares coking heater with existing old process feeding temperature can drop to below 350 ℃ by 390 ℃, and it is few to contain coke powder, and therefore the radiation fresh feed pump severity as one of coker nucleus equipment can reduce.Can reduce investment outlay like this and the prolonged operation expense.
The concrete data of effect free list 1～table 3 of the present invention further specify.
Table 1 has been listed the comparison of the old process of introducing in flow process of the present invention and the background technology;
Table 2 is listed recycle ratio and is respectively the product yield under 0.25 and 0.1 situation and the comparison of benefit;
Table 3 has been listed investment and the process cost and the investment of the delayed coking unit of one 1,000,000 tons/year of employing old process construction and the comparison of process cost that adopts flow process of the present invention to build one 1,000,000 tons/year delayed coking unit, is benchmark with the old process.
From table 1, as can be seen, adopt flow path device of the present invention to have flexibility of operation preferably, device can change product yield according to different demands, increases economic efficiency.By table 2, table 3 as can be seen, though adopt apparatus of the present invention facility investment to increase by 3,800,000 yuan, but under identical condition, if recycle ratio is dropped to 0.1 by 0.25, to the device of 1,000,000 tons of/year scales only the variation of product yield can increase by 1,119 ten thousand yuan/year of benefits, process cost also reduces 54.7 ten thousand yuan/year, can recoup capital outlay in about 4 months.
Describe the present invention in detail below in conjunction with accompanying drawing, but accompanying drawing does not limit concrete enforcement of the present invention.
Description of drawings:
Accompanying drawing is a typical process synoptic diagram of the present invention.
Embodiment:
As shown in the figure: from the incoming stock surge tank 2 of the coking raw material of pipeline 1, after feedstock pump 3 boosts, enter heat-exchange system 4, heat exchange enters coking heater charging surge tank 5 after 200-350 ℃.Coking heater charging 6 is retracted to coking heater 8 through radiation fresh feed pump 7 and is heated to 495-505 ℃ and enters coke drum 9, reaction oil gas 11 advances coking fractional distillation column 12, turning oil 18 is extracted out from coking fractional distillation column 12 bottoms by circulating oil pump 13, the turning oil 18 of extraction after water cooler 14 coolings, be divided into three the tunnel: the one tunnel for refluxing 19 to return coking fractional distillation column 12 bottoms, a tunnel be that coking recycle oil 17 mixes with coking raw material 1, the one tunnel is that product 20 goes out device.Refluxed among the figure 19 minutes two the tunnel and return coking fractional distillation column 12 bottoms: on reflux and 15 beat on the heat exchange baffle plate 10 as the backflow of control oil gas temperature, the following backflow 16 got to coking fractional distillation column 12 bottom liquid phases as controlling at the bottom of the separation column backflow of liquidus temperature.Among the figure coking recycle oil 17 and coking raw material 1 mix can according to raw material different qualities, carry out to the optional position between the furnace charge surge tank 5 at above-mentioned pipeline 1.
Table-1
| Project | Flow process of the present invention | Old process |
| Technological process adaptability | Good | Generally |
| The fractionating column coking | Be difficult for | Easily |
| Radiation feeding belt coke powder | Few | Many |
| Recycle ratio | 0～1.0 | 0.25-0.40 |
| The green coke amount | Few | Many |
| The compressor operation load | Little | Greatly |
Table-2
Annotate: product price is pressed: 2934 yuan/tons in gasoline, 2485 yuan/tons of diesel oil, 2087 yuan/tons of wax oils,
| Project | Product yield % | Poor yields (percentage point) | By 1,000,000 ton/years of scales, output poor (ten thousand ton/years) | (ten thousand yuan) of poor benefits | |
| Recycle ratio 0.1 | Recycle ratio 0.25 | ||||
| Dry gas | 5.61 | 5.90 | -0.29 | -0.29 | -377 |
| Liquefied gas | 2.40 | 2.53 | -0.13 | -0.13 | -324 |
| Gasoline | 12.47 | 13.14 | -0.67 | -0.67 | -1966 |
| Diesel oil | 25.30 | 27.34 | -2.04 | -2.04 | -5069 |
| Wax oil | 24.69 | 20.26 | +4.43 | +4.43 | +9245 |
| Coke | 27.83 | 29.13 | -1.30 | -1.30 | -390 |
| Amount to | +1119 | ||||
300 yuan/tons in coke, 1300 yuan/tons of dry gas, 2494 yuan/tons of calculating of liquefied gas.
Table-3
| Sequence number | Project | Flow process of the present invention | Old process | Remarks |
| One | Equipment investment | |||
| 1 | Heat exchanger | 1,740,000 yuan | 0 | |
| 2 | Pump | 1,000,000 yuan | 0 | Two oil-slurry pumps |
| 3 | The furnace charge surge tank | 440,000 yuan | 0 | |
| 4 | Pipeline, valve, insulation | 620,000 yuan | 0 | |
| 3 | Subtotal | 3,800,000 yuan | ||
| Two | Operating cost | |||
| 1 | Pump power consumption kW | 97 | 0 | |
| 2 | RMB is amounted in the electricity charge | 48.1 ten thousand yuan/year | 0 | 0.62 unit/degree |
| 3 | Fuel consumption | -494kg/h, consider device heat recovery rate 80%, then saving-98.8kg/h | 0 | Recycle ratio reduces by 0.15 and causes the minimizing that heating furnace is loaded |
| 4 | Fuel saving is amounted to RMB | -102.8 ten thousand yuan/year | 0 | 1300 yuan/tons of fuel |
| 5 | The operating cost subtotal | -54.7 ten thousand yuan/year | 0 |
Claims (6)
- But 1, a kind of delay coking process of flexible recycle ratio operation, it is characterized in that: coking raw material and following coking recycle oil are mixed into coking heater, after being heated to coking temperature, enter coke drum and carry out thermally splitting and condensation reaction, reaction oil gas advances coking fractional distillation column, the coking fractional distillation column bottom is extracted turning oil out, turning oil is after the heat exchange cooling, a part is returned the coking fractional distillation column bottom as backflow, and a part is mixed with above-mentioned coking raw material as coking recycle oil or/and a part goes out device as product.
- 2, according to the described delay coking process of claim 1, it is characterized in that: described coking recycle oil mixes with coking raw material after filtering through filter again.
- 3, according to claim 1 or 2 described delay coking process, it is characterized in that: described coking recycle oil and mixing of coking raw material are to entering any one position on pipeline between the coking heater or the equipment at the coking raw material motion device.
- 4, according to claim 1 or 2 described delay coking process, it is characterized in that: the feeding temperature of coking heater is 200-350 ℃.
- 5, according to claim 1 or 2 described delay coking process, it is characterized in that: the circulation oil content two tunnel of backflow returns coking fractional distillation column, and one the tunnel returns heat exchange baffle plate top in the coking fractional distillation column, and coking fractional distillation column bottom liquid phase is returned on another road.
- 6, according to claim 1 or 2 described delay coking process, it is characterized in that: establish the charging buffer device before the coking heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021393125A CN1189540C (en) | 2002-07-11 | 2002-07-11 | Delay coking process able to flexibly regulate recirculating ratio |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021393125A CN1189540C (en) | 2002-07-11 | 2002-07-11 | Delay coking process able to flexibly regulate recirculating ratio |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1396236A true CN1396236A (en) | 2003-02-12 |
| CN1189540C CN1189540C (en) | 2005-02-16 |
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ID=4750024
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021393125A Expired - Lifetime CN1189540C (en) | 2002-07-11 | 2002-07-11 | Delay coking process able to flexibly regulate recirculating ratio |
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| Country | Link |
|---|---|
| CN (1) | CN1189540C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102373080A (en) * | 2010-08-19 | 2012-03-14 | 中国石油化工股份有限公司 | Coking delaying method |
| CN102533320A (en) * | 2010-12-30 | 2012-07-04 | 中国石油化工股份有限公司 | Processing method of heavy oil with high asphaltene content |
| CN102816587A (en) * | 2011-06-07 | 2012-12-12 | 中国石油化工集团公司 | Full wax oil under-refluxing overheat-removing and circulation ratio quantitative controlling coking-retarding apparatus and method |
| CN104099124A (en) * | 2013-04-15 | 2014-10-15 | 中石化洛阳工程有限公司 | Test method for on-line circulation of delayed coking cycle oil |
| CN104774638A (en) * | 2015-03-30 | 2015-07-15 | 广东石油化工学院 | Method for avoiding shot coke generation in inferior residuum processing |
| CN113684051A (en) * | 2021-08-30 | 2021-11-23 | 辽宁宝来生物能源有限公司 | Circulating oil temporary storage system for oil-based needle coke production |
-
2002
- 2002-07-11 CN CNB021393125A patent/CN1189540C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102373080A (en) * | 2010-08-19 | 2012-03-14 | 中国石油化工股份有限公司 | Coking delaying method |
| CN102533320A (en) * | 2010-12-30 | 2012-07-04 | 中国石油化工股份有限公司 | Processing method of heavy oil with high asphaltene content |
| CN102533320B (en) * | 2010-12-30 | 2014-07-30 | 中国石油化工股份有限公司 | Processing method of heavy oil with high asphaltene content |
| CN102816587A (en) * | 2011-06-07 | 2012-12-12 | 中国石油化工集团公司 | Full wax oil under-refluxing overheat-removing and circulation ratio quantitative controlling coking-retarding apparatus and method |
| CN102816587B (en) * | 2011-06-07 | 2014-12-17 | 中国石油化工集团公司 | Full wax oil under-refluxing overheat-removing and circulation ratio quantitative controlling coking-retarding apparatus and method |
| CN104099124A (en) * | 2013-04-15 | 2014-10-15 | 中石化洛阳工程有限公司 | Test method for on-line circulation of delayed coking cycle oil |
| CN104774638A (en) * | 2015-03-30 | 2015-07-15 | 广东石油化工学院 | Method for avoiding shot coke generation in inferior residuum processing |
| CN113684051A (en) * | 2021-08-30 | 2021-11-23 | 辽宁宝来生物能源有限公司 | Circulating oil temporary storage system for oil-based needle coke production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1189540C (en) | 2005-02-16 |
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Owner name: SINOPEC LUOYANG ENGINEERING CO., LTD. Free format text: FORMER NAME: CHINA PETROCHEMICAL CORPORATION |
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| CP01 | Change in the name or title of a patent holder |
Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee after: LUOYANG PETROCHEMICAL ENGINEERING CORPORATION, SINOPEC Address before: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee before: Luoyang Petrochemical Engineering Co.,Ltd./SINOPEC |
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Granted publication date: 20050216 |
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