CN103725306B - The separation method and device of reforming reaction product - Google Patents
The separation method and device of reforming reaction product Download PDFInfo
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- CN103725306B CN103725306B CN201210381501.XA CN201210381501A CN103725306B CN 103725306 B CN103725306 B CN 103725306B CN 201210381501 A CN201210381501 A CN 201210381501A CN 103725306 B CN103725306 B CN 103725306B
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Abstract
The present invention relates to the separation method and device of reforming reaction product, more particularly to reforming reaction hydrogen product Isolation method.Mainly include the following steps that：Reforming reaction product（1）Fed with reforming reaction（2、3）Heat exchange（4）Afterwards, it is directly entered the pre-separation tank set up（7）, pre-separation gas phase（9）Again by air cooling（11）Enter follow-up knockout drum after cooling（12）Contact portion, isolates recycle hydrogen again（13）And high-purity hydrogen, pre-separation liquid phase（10）Then with contact tank liquid phase again（8）Follow-up fractionating section is directly entered after mixing.The present invention reduces the flow for repeating cooling, intensification logistics, the heating load of fractionating section is reduced, while alleviating the underload contradiction of summer air cooling, compared with prior art, the present invention reduces cooling load 14.5%, reduces heating load 18.2%, and energy-saving effect is notable.
Description
Technical field
The invention belongs to refining process's reforming reaction product separation technology field, more particularly to reforming reaction product point
From B-grade condensation separation method.
Background technology
Reforming process is the important process in oil refining and petrochemical industry, is mainly used to produce high-knock rating gasoline or weight
Industrial chemicals benzene, paraxylene for wanting etc..Reforming reaction temperature is higher, is 380 ~ 520 DEG C, reforming reaction product and the weight of high temperature
After whole reaction feed heat exchange, still there are 90 ~ 110 DEG C.Product now is in gas-liquid two-phase state, in order in isolating product
Hydrogen recycle and send outside, current domestic all of reformer will be reacted using air cooling in production or design, and be produced
After thing temperature is reduced to 30 ~ 50 DEG C, enter back into follow-up separation, again contact portion isolate the hydrogen of recycle hydrogen and high-purity.
The reformation oil temperature that above-mentioned flow is obtained is 40 DEG C or so, and follow-up fractional distillation process need to be warming up to reformate it is higher
Temperature（150~190 DEG C）, so repeat cooling-heating process and not only consume substantial amounts of cooling load, also increase follow-up
The heating load of flow.
At present, there are obvious power savings advantages using B-grade condensation separation process in hydrogeneous logistics gas-liquid refrigerated separation method,
For example in oil refining process the product refrigerated separation of hydro-refining unit and hydrocracking unit is had and is separated using thermal high
Flow.
B-grade condensation separate refer to gas-liquid mixed logistics once exchange heat recovery heat after, not directly enter cooler and be cooled to
Technological requirement temperature, but gas-liquid separation is carried out into a knockout drum, it is necessary to further the gas phase of cooling enters back into cooler
Technological temperature is cooled to, the liquid phase for being not required to cooling is then directly entered follow-up process.
, according to the process characteristic of reforming reaction product separate section, temperature is between 90~120 DEG C, pressure after heat exchange for the present invention
Reforming reaction product gas-liquid separation between 0.24~0.26MPag uses Isolation method, it is to avoid reformate repeats to cool down-add
Heat causes energy loss, and heat is fully recycled.Pre-separation flow reduces the cooling load of reforming reaction air cooler with after
The heating load of continuous separate section, can significantly reduce process energy consumption, with significantly more characteristics of energy saving.
The present invention repeats cooling-heating problems to solve reforming reaction product, is produced reforming reaction using Isolation method
Thing is pre-separated out and is not required to cooling logistics and need to cool down logistics, and it is pre-separation tank liquid phase to be not required to cooling logistics, direct without cooling
Into follow-up separate section；Logistics need to be cooled down for pre-separation tank gas phase, 40 DEG C or so are cooled to by air cooler, enter back into weight
Whole product knockout drum and again contact portion；Pre-separation tank liquid phase mixes rear temperature for 60 ~ 110 DEG C with Fluid Contacting again, fills
Divide the heating load for reducing later separation part.
The content of the invention
It is an object of the invention to provide a kind of reforming reaction product separation method based on pre-separation flow.Skill of the present invention
Art scheme avoids the repetition cooling-heating of reformate, reduces the heating load of cooling load and downstream processes, reduces dress
The energy consumption put.
The present invention relates to following proposal：
Scheme 1, a kind of separation method of the reforming reaction product based on pre-separation technique, the method include B-grade condensation point
From step, before reforming reaction product enters reforming reaction product knockout drum, with reforming reaction product pre-separation tank
Pre-separation step.
Scheme 2, according to the methods described of aforementioned schemes 1, wherein reforming reaction product is isolated after pre-separation needs cooling
Logistics（9）（I.e. pre-separation gas phase, main to constitute as C1~C5Lighter hydrocarbons and hydrogen）Be not required to cool down logistics（10）（That is pre-separation liquid
Phase, main composition is C5Reformate above）.
Scheme 3, according to the methods described of aforementioned schemes 1 or 2, wherein reforming reaction product（1）Fed with reforming reaction（2,3）
After heat exchange, reforming reaction product pre-separation tank is entered without cooling（7）Carry out gas-liquid separation.
Scheme 4, according to aforementioned schemes any one methods described, wherein product pre-separation tank（7）Temperature for 90 ~
Between 110 DEG C, pre-separation pressure tank is 0.24 ~ 0.26MPa.
Scheme 5, according to aforementioned schemes any one methods described, the wherein gas phase of pre-separation tank（9）It is cooled to by air cooling
Enter reforming reaction product knockout drum after 30 ~ 50 DEG C（12）Further gas-liquid separation.
Scheme 6, according to aforementioned schemes any one methods described, wherein reforming reaction product knockout drum（12）Pressure is 0.23
~0.25MPa。
Scheme 7, according to aforementioned schemes any one methods described, the wherein gas phase of pre-separation tank（9）Enter after supercooling
Reforming reaction product knockout drum（12）Further gas-liquid separation.
Scheme 8, according to aforementioned schemes any one methods described, wherein pre-separation tank liquid phase（10）With No. 1 contact tank liquid again
Phase（8）Enter follow-up fractionating section after mixing（18）.
Scheme 9, reforming reaction product separator, it is before reforming reaction product enters reforming reaction product knockout drum
Including B-grade condensation equipment, such as reforming reaction product pre-separation tank and reforming reaction product knockout drum.
Scheme 10, the device according to scheme 9, it is used to implement any one method of aforementioned schemes 1 ~ 8.
Specifically, according to a kind of specific embodiment of the invention, reforming reaction product is exchanged heat with reforming reaction charging
To after 90~110 DEG C, the pre-separation tank set up is directly entered, carries out gas-liquid separation；By pre-separation tank gas phase（Main composition is C1
~C5Lighter hydrocarbons and hydrogen）Draw, 30 ~ 50 DEG C are cooled to by air cooling, entering back into reformate knockout drum carries out gas-liquid separation；
Pre-separation tank liquid phase（Main composition is C5Reformate above）With No. 1 after contact tank liquid phase mixes again, be directly entered fractionation portion
Point.
According to another kind specific embodiment of the invention, the inventive method is suitable for fixed bed semi regeneration and reforms, circulates again
Raw reformation and the reforming reaction product gas-liquid separation technique of continuous reforming process device, such as following reforming reactions, its
Middle reforming reaction pressure is 0.3-0.5MPa, and reaction temperature is 380-520 DEG C, and reforming reaction product is laggard by exchanging heat, cooling down
Enter it is follow-up contact again, separate section, isolate recycle hydrogen and high-purity hydrogen（For example, purity is more than 90mol%）Profit of the invention
Being pre-separated out reforming reaction product with Isolation method need to cool down logistics and be not required to cool down logistics, be not required to cool down logistics ---
Pre-separation liquid phase is directly entered fractionating section after contact tank liquid phase mixes again with No. 1, reduce cooling load and follow-up process plus
Thermic load；Logistics need to be cooled down --- pre-separation gas phase after air cooling cooling by entering reforming reaction product knockout drum.Pre-separation liquid
Be 60 ~ 90 DEG C with No. 1 temperature after contact tank liquid phase mixes again, more original be only No. 1 of 40 DEG C again contact tank liquid phase it is direct
Into fractionating section, 20 ~ 50 DEG C are improve, greatly reduce the heating energy consumption of subsequent fractionation part.
Brief description of the drawings
Accompanying drawing 1 is a kind of specific embodiment of technical process that Isolation method of the invention separates reforming reaction product
Schematic diagram.Wherein reference is as follows：
1st, reforming reaction product, 2, recycle hydrogen, 3, refined naphtha, 4, plate type heat exchanger, 5, reforming reaction charging, 6, change
Reforming reaction product after heat, 7, pre-separation tank, 8, contact liquid phase again, 9, pre-separation gas phase, 10, pre-separation liquid phase, 11, air cooling
Device, 12, reformate knockout drum, 13, knockout drum gas phase, 14, knockout drum liquid phase, 15, reforming reaction heating furnace, 16, recycle hydrogen
Compressor, 17, contact portion again, 18, fractionating section.In non-limiting manner, the flow general introduction according to the methods described of accompanying drawing of the present invention 1
It is as follows：Reforming reaction product（1）Fed with reforming reaction（2,3）After heat exchange, pre-separation tank is directly entered without cooling（7）Carry out
Gas-liquid separation, pre-separation tank gas phase（9）Again by air cooling（11）It is cooled to technological requirement temperature（30~50℃）Enter afterwards and reform instead
Answer product knockout drum（12）, knockout drum gas phase（13）Into follow-up compressor（16）Boosting, knockout drum liquid phase（14）Then enter
Follow-up contact portion again（17）, pre-separation tank liquid phase（10）With contact liquid phase again（8）（Separate the reformate after hydrogen）It is mixed
Enter follow-up fractionating section after conjunction（18）.
Specific embodiment
It is explained further the present invention with reference to embodiments, but embodiment does not do any type of limit to the present invention
It is fixed.
By taking 800,000 tons/year of continuous reformers of oil plant as an example, pre-separation flow of the present invention is illustrated.This device uses UOP
Coaxial continuous reforming process, reforming reaction temperature is 380 ~ 520 DEG C, and pressure is 0.34 ~ 0.45MPa, and product is first board-like
Heat exchanger exchanges heat to after 100 ~ 120 DEG C with reforming reaction charging, then is cooled to 40 DEG C or so by air cooling, divides into follow-up
From, again contact portion separate recycle hydrogen and high-purity hydrogen.Reforming reaction product analysis composition data is as shown in table 1.
The reforming reaction product analysis of table 1 are constituted, %
| Carbon number | Alkane | Cycloalkane | Aromatic hydrocarbons |
| C1 | 11.91 | - | - |
| C2 | 2.38 | - | - |
| C3 | 0.0013 | - | - |
| C4 | 0.039 | - | - |
| C5 | 7.71 | 0.58 | - |
| C6 | 10.58 | 4.64 | 3.56 |
| C7 | 7.51 | 8.30 | 3.37 |
| C8 | 8.12 | 8.14 | 7.26 |
| C9 | 5.56 | 5.67 | 1.08 |
| C10 | 2.94 | 0.64 | - |
Temperature is 106 DEG C after original uses full condensation separation flow, reforming reaction product to be exchanged heat with reaction feed, cold through air cooling
But reformate knockout drum is entered to 40 DEG C, pressure is 0.26MPag, cooling logistics flux is 100100kg/h, is counted through simulation
Calculate, its cooling load is 9.66MW；Through after the hydrogen that contact portion again isolates high-purity, the reformation oil temperature for obtaining is 40
DEG C, and reformate heat exchange need to be warmed up to 173 DEG C by downstream fractionation part, need heating load 7.57MW.
The present invention is pre-separation flow, and pre-separation tank is set up on the basis of former full condensation separation flow, and reforming reaction is produced
After the charging heat exchange of thing and reforming reaction, pre-separation tank is directly entered without cooling, pressure is 0.26MPag, through gas-liquid separation after,
Pre-separation gaseous stream flow is 69800kg/h, and 40 DEG C are cooled to through air cooling, and its refrigeration duty is 8.26MW；Pre-separation liquid phase thing
Stream flow is 30300kg/h, is 64 DEG C with the mixed temperature of contact tank liquid phase again, and more original logistics improves 24 DEG C, presses
173 DEG C of calculations are still warming up to, the heating load that subsequent fractionation part needs is 6.19MW.Before being transformed by B-grade condensation separation process
Hydrogen purity is contacted again afterwards to such as table 2.
Table 2 optimizes front and rear hydrogen purity contrast
| Component | H2 | C1 | C2 | C3 | C4 | C5 | |
| Before transformation | 91.66 | 6.10 | 1.63 | 0.26 | 0.0032 | 0.17 | 40000 |
| After transformation | 91.38 | 6.17 | 1.69 | 0.30 | 0.0049 | 0.23 | 40300 |
By more than analyze, using pre- hydrogenation products separation process of the invention after, cooling load can be reduced
1.40MW, saves 14.5%, while alleviating the underload contradiction of summer air cooling；Reduce subsequent fractionation part heating load
1.38MW, saves 18.2%.
Claims (8)
1. the separation method of the reforming reaction product of pre-separation technique is based on, and the method includes B-grade condensation separating step, in weight
Before whole product enters reforming reaction product knockout drum, the pre-separation step with reforming reaction product pre-separation tank, its
Middle reforming reaction product is isolated after pre-separation and need to cool down logistics（9）, i.e. pre-separation gas phase, and be not required to cool down logistics
（10）, i.e. pre-separation liquid phase, wherein reforming reaction product（1）Fed with reforming reaction（2,3）After heat exchange, weight is entered without cooling
Whole product pre-separation tank（7）Carry out gas-liquid separation, wherein product pre-separation tank（7）Temperature for 90 ~ 110 DEG C it
Between, pre-separation pressure tank is 0.24 ~ 0.26MPa.
2., according to the methods described of preceding claims 1, the wherein gas phase of pre-separation tank enters after air cooling is cooled to 30 ~ 50 DEG C
Reforming reaction product knockout drum（12）Further gas-liquid separation.
3., according to the methods described of preceding claims 1 or 2, it is 0.23 ~ 0.25MPa that wherein reforming reaction product separates pressure tank.
4., according to the methods described of preceding claims 1 or 2, wherein the gas phase of pre-separation tank is produced after supercooling into reforming reaction
Thing knockout drum（12）Further gas-liquid separation.
5. according to the methods described of preceding claims 1 or 2, wherein pre-separation tank liquid phase and No. 1 contact tank liquid phase again（8）After mixing
Into follow-up fractionating section（18）.
6. reforming reaction product separator, it included two grades before reforming reaction product enters reforming reaction product knockout drum
Condensing plant, wherein product pre-separation tank（7）Temperature between 90 ~ 110 DEG C, pre-separation pressure tank is 0.24 ~
0.26MPa。
7. device according to claim 6, it is used to implement any one method of preceding claims 1 ~ 5.
8. device according to claim 6, wherein B-grade condensation equipment are selected from reforming reaction product pre-separation tank and reforming reaction
Product knockout drum.
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| CN201210381501.XA CN103725306B (en) | 2012-10-10 | 2012-10-10 | The separation method and device of reforming reaction product |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105712815A (en) * | 2014-12-05 | 2016-06-29 | 中国石油化工股份有限公司 | Energy saving separation method |
| CN105712814A (en) * | 2014-12-05 | 2016-06-29 | 中国石油化工股份有限公司 | Improved separation method |
| CN105441118B (en) * | 2015-12-10 | 2018-07-27 | 上海优华系统集成技术股份有限公司 | A kind of recycling reformation contacts the method and device of cold again |
| CN108239553B (en) * | 2016-12-23 | 2020-06-09 | 中国石油天然气集团有限公司 | Reforming reaction product separation system and method |
| CN112708482B (en) * | 2020-12-28 | 2023-05-05 | 山东京博石油化工有限公司 | Fixed bed reformate treatment system and treatment method |
Citations (3)
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|---|---|---|---|---|
| EP1624041A1 (en) * | 2004-08-03 | 2006-02-08 | Hitachi, Ltd. | System for reforming heavy oil , method thereof, and combined cycle power system |
| CN1923972A (en) * | 2006-09-06 | 2007-03-07 | 中国石油化工集团公司 | Hydrocarbons hydrocracking method |
| CN102465014A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrocracking method for processing low-sulfur raw material |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1624041A1 (en) * | 2004-08-03 | 2006-02-08 | Hitachi, Ltd. | System for reforming heavy oil , method thereof, and combined cycle power system |
| CN1923972A (en) * | 2006-09-06 | 2007-03-07 | 中国石油化工集团公司 | Hydrocarbons hydrocracking method |
| CN102465014A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrocracking method for processing low-sulfur raw material |
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Address after: 100728 Chaoyangmen North Street, Chaoyang District, Chaoyang District, Beijing Co-patentee after: Sinopec Consulting Co.,Ltd. Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Address before: 100728 Chaoyangmen North Street, Chaoyang District, Chaoyang District, Beijing Co-patentee before: SINOPEC CONSULTING Co. Patentee before: CHINA PETROLEUM & CHEMICAL Corp. |
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Effective date of registration: 20181127 Address after: 100728 Chaoyangmen North Street, Chaoyang District, Chaoyang District, Beijing Co-patentee after: SINOPEC ENERGY SAVING TECHNOLOGY SERVICE Co.,Ltd. Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Address before: 100728 Chaoyangmen North Street, Chaoyang District, Chaoyang District, Beijing Co-patentee before: Sinopec Consulting Co.,Ltd. Patentee before: CHINA PETROLEUM & CHEMICAL Corp. |