CN1053691C - Hydrogenation technology - Google Patents
Hydrogenation technology Download PDFInfo
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- CN1053691C CN1053691C CN 96115495 CN96115495A CN1053691C CN 1053691 C CN1053691 C CN 1053691C CN 96115495 CN96115495 CN 96115495 CN 96115495 A CN96115495 A CN 96115495A CN 1053691 C CN1053691 C CN 1053691C
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Abstract
The present invention relates to a hydrogenation technology which belongs to the field of oil refining chemical industry. The present invention changes a high pressure heat exchanger in the traditional hydrogenation technology into a low pressure heat exchanger makes high pressure equipment such as a high pressure separator, a high pressure cooler, etc. and pipelines grouped at an outlet of a reactor, which is convenient for safety management and has the advantages of safety coefficient increase, high pressure equipment and pipeline saving and low investment.
Description
The invention belongs to the oil-refining chemical field, particularly a kind of high-pressure hydrogenation process.
The oil of China is becoming heavy gradually, and impure sulphur, nitrogen, oxygen amount are more and more many, hydrogenation technique to improve the quality of products, aspects such as heavy oil lighting and environment protection play a positive role.In general, hydrogenation technique device high-pressure system is by reactor, and process furnace, hydrogen pressure machine, high-pressure separator, water cooler, interchanger, high-pressure pump and pipeline are formed, belong to high-temperature high-pressure apparatus, safety coefficient is lower, the material of high-pressure system equipment is had relatively high expectations the investment cost costliness.
It is lower to the present invention is directed to the hydrogenation technique safety coefficient, and the shortcoming of investment cost costliness proposes a kind of new high-pressure hydrogenation process.
The present invention program is: (1) resultant of reaction directly advances first high-pressure separator from reactor outlet, go into the oily into MP (medium pressure) separator of coming out from first high-pressure separator bottom, generate oil and come out to enter low pressure interchanger and stock oil heat exchange by the MP (medium pressure) separator bottom, also can partly adopt high pressure heat exchanger according to feedstock property, all the other adopt the low pressure parallel operation, generation oil after the heat exchange enters light pressure separator, the generation oil of isolating behind the gas such as hydrogen enters separation column, and the flow process behind the separation column is with the hydrogenation loading amount is identical at present; (2) gas that comes out from first high-pressure separator top enters HP cooler tube side and water coolant heat exchange, liquid and hydrogen after being come out by HP cooler enter second high pressure from device, and liquid comes out to enter fractionation cat head or direct admission oil tank from second high-pressure separator bottom; (3) after the stock oil behind the access to plant is boosted by low-pressure pump, enter the intermediate raw material jar by deep fat at the bottom of low pressure interchanger and the tower with after generating oily heat exchange, stock oil advances the high pressure feedstock pump by the intermediate raw material pot bottom, is mixed into process furnace with hydrogen after high-pressure pump rises to required pressure.
The present invention compares with present hydrogenation technique, it is characterized in that:
1, high-pressure system is only limited to sub-fraction, and technical process is simplified in favourable management;
2, because high-pressure separator has two, establish one or two safety valve on every platform, the increase safety coefficient also can be established as required and pine for pressing separator;
3, replace high pressure heat exchanger with the low pressure interchanger, save the investment of high pressure heat exchanger and high pressure line.
4, the gas at high-pressure separator top can be walked tube side through cooling, and the cooler casing pressure rating can be used low pressure.
5, the low pressure heat exchange process is all adopted in the heat exchange of stock oil and generation oil, and setting device intermediate raw material jar, helps removing of raw water and non-condensable gas.
6, mix the hydrogen place and be located on the pipeline of high-pressure pump back, then directly advance process furnace.
7, because first high-pressure separator so the vaporization of part light oil is arranged, is returned and combined in second high-pressure separator and put the load that has reduced mesolow separator and separation column, and reduced the investment of mesolow separator and separation column, useful to quiet run simultaneously.
8, this technology has been avoided generation oil to enter behind the cold high-low pressure separator through heat exchange again and has been utilized process furnace, and the fractionated flow process of tower is advanced in heating, and is useful to energy recovery and energy conservation, and reduces by a process furnace.
9, this technology can partly adopt high pressure heat exchanger according to feedstock property, and all the other all adopt the low pressure interchanger.
Accompanying drawing is a process flow sheet of the present invention.
Below in conjunction with accompanying drawing the present invention is elaborated.
Resultant of reaction directly enters high-pressure separator (1) from reactor outlet A, generating oil comes out from high-pressure separator (1) bottom to enter MP (medium pressure) separator (4) below 1/2 by what control valve was decompressed to system pressure, generating oil comes out to be decompressed to below the 2.0MPa by MP (medium pressure) separator (4) bottom, enter low pressure interchanger (5) and stock oil heat exchange, low pressure interchanger platform number can be provided with some according to going into the tower temperature, also can be according to feedstock property, part adopts high pressure heat exchanger, generation oil after the heat exchange enters separation column C2 by light pressure separator (9), and the flow process behind the separation column is with hydrogenation unit is identical at present.
The gas that comes out from high-pressure separator (1) top, certain light oil is contained in inside, enter HP cooler (2) tube side and water coolant heat exchange, enter high-pressure separator (3) behind liquid after coming out by HP cooler (2) and the hydrogen, liquid enter after from high-pressure separator (3) bottom by the control valve decompression separation column C1 return stream with or direct admission oil tank D.
The gas that comes out from high-pressure separator (2) top enters circulating hydrogen compressor B inlet and divides flow container to recycle; If reacted oil vaporization rate under this condition seldom can not established high-pressure separator (2).
After stock oil behind the access to plant is boosted by low-pressure pump (11), enter intermediate raw material jar (6) by low pressure interchanger (10), low pressure interchanger (5) with deep fat at the bottom of the tower with after generating oily heat exchange, stock oil advances high pressure feedstock pump (8) by intermediate raw material jar (6) bottom, after high pressure feedstock pump (8) rises to required pressure mixed hydrogen place (7) with enter process furnace H after hydrogen mixes.Flow process is only drawn and present hydrogenation unit technology difference among the figure, some of them valve etc. does not all draw, and interchanger platform number is not determined, be because the required condition difference of different material hydrogenation is temperature, pressure difference, the gas content on high-pressure separator top is relevant with reaction depth, so the water cooler area can be decided according to stock oil character and purpose product.
The explanation in attached picture in picture footpath: A-reactor B-circulating hydrogen compressor C1, C2, C3,---tower D-gasoline cistern E---new hydrogen system---gas net G---removes to cool off H---and goes to add for system F1, F2 Hot stove J---goes out device K---raw material.
Claims (2)
1, a kind of hydrogenation technique is characterized in that:
(1) reaction generation oil directly advances first high-pressure separator (1) from reactor outlet, generating oil comes out from first high-pressure separator (1) bottom to enter MP (medium pressure) separator (4) below 1/2 by what control valve was decompressed to system pressure, generating oil comes out to reduce pressure below the 2.0MPa by the MP (medium pressure) separator bottom, enter low pressure interchanger (5) and stock oil heat exchange, generation oil after the heat exchange enters light pressure separator (9), and the generation oil of isolating behind the gases such as hydrogen enters separation column c
2, separation column c
2After flow process with at present hydrogenation unit is identical;
(2) gas that comes out from first high-pressure separator (1) top, enter HP cooler tube side (2) and water coolant heat exchange, liquid and hydrogen after being come out by HP cooler (1) enter second high-pressure separator (3), and liquid enters separation column c from second high-pressure separator (3) bottom after by the control valve decompression
1Or direct admission oil cylinder D, the gas that comes out from second high-pressure separator (3) top enters circulating hydrogen compressor B inlet;
(3) after the stock oil behind the access to plant is boosted by low-pressure pump (11), enter intermediate raw material jar (6) by low pressure interchanger (10), (5) with deep fat at the bottom of the tower with after generating oily heat exchange, high pressure feedstock pump (8) is advanced in head tank between stock oil Tanaka (6) bottom, enters process furnace after high-pressure pump rises to required pressure with after hydrogen mixes.
2, as the said hydrogenation technique of claim 1, it is characterized in that said interchanger to gasoline hydrogenation technology, can adopt high pressure heat exchanger to adopt the heat exchange of low pressure interchanger more earlier.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96115495 CN1053691C (en) | 1996-07-25 | 1996-07-25 | Hydrogenation technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96115495 CN1053691C (en) | 1996-07-25 | 1996-07-25 | Hydrogenation technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1172146A CN1172146A (en) | 1998-02-04 |
| CN1053691C true CN1053691C (en) | 2000-06-21 |
Family
ID=5122741
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96115495 Expired - Fee Related CN1053691C (en) | 1996-07-25 | 1996-07-25 | Hydrogenation technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1053691C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100351346C (en) * | 2004-07-14 | 2007-11-28 | 中国石油化工股份有限公司 | Medium pressure hydrocracking process for preparing jet fuel |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098332C (en) * | 2000-08-25 | 2003-01-08 | 中国科学院兰州化学物理研究所 | Method of reducing olefin and benzene content in gasoline |
| CN101168685B (en) * | 2006-10-26 | 2010-11-03 | 中国石油天然气股份有限公司 | Device and technique for increasing circulation hydrogen concentration of high-pressure hydrogenation reactor |
| US8424181B2 (en) * | 2009-04-17 | 2013-04-23 | Exxonmobil Research And Engineering Company | High pressure revamp of low pressure distillate hydrotreating process units |
| CN105542837A (en) * | 2015-12-15 | 2016-05-04 | 北京中科诚毅科技发展有限公司 | Step-by-step pressure reduction method of three-phase fluid as well as design method and application thereof |
| CN113122314B (en) * | 2019-12-31 | 2022-07-12 | 中国石油化工股份有限公司 | Gas-liquid separation process for hydrogenation reaction product |
-
1996
- 1996-07-25 CN CN 96115495 patent/CN1053691C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100351346C (en) * | 2004-07-14 | 2007-11-28 | 中国石油化工股份有限公司 | Medium pressure hydrocracking process for preparing jet fuel |
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| Publication number | Publication date |
|---|---|
| CN1172146A (en) | 1998-02-04 |
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