CN101092570B - Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon - Google Patents
Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon Download PDFInfo
- Publication number
- CN101092570B CN101092570B CN2006100869741A CN200610086974A CN101092570B CN 101092570 B CN101092570 B CN 101092570B CN 2006100869741 A CN2006100869741 A CN 2006100869741A CN 200610086974 A CN200610086974 A CN 200610086974A CN 101092570 B CN101092570 B CN 101092570B
- Authority
- CN
- China
- Prior art keywords
- oil
- heavy
- gas
- quencher
- oil gas
- 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.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
This invention discloses a method for separating high-temperature catalytically cracked oil gas rich in light hydrocarbons and catalyst dust. The method comprises: performing countercurrent direction contact between high-temperature reaction oil gas containing catalyst dust and the catalytically cracking raw material in a quench cooler to cool the high-temperature reaction oil gas and heat the catalytically cracking raw material, pumping out oil slurry containing catalyst dust, pumping out diesel oil fraction via a rectification column, and separating light hydrocarbons and gasoline fraction via a water-washing column. The method has such advantages as high heat-exchange efficiency, low cooling load at the overhead of the main rectification column, low pressure drop from the reaction oil gas to the inlet of the gas compressor, low energy consumption of the gas compressor, low coking at the bottoms of the quench cooler and the rectification column, and no emulsion phenomenon of the materials at the overhead of the main rectification column.
Description
Technical field
The present invention relates to the separation method of catalytic cracking petroleum hydrocarbons product, more particularly, relate to a kind of C of being rich in
2～C
4Hydro carbons and carry the separation method of the high-temperature catalytic crackate of catalyst dust.
Background technology
The traditional method of utilizing petroleum hydrocarbon to produce ethene, propylene is a steam cracking, and the raw material of employing is ethane, Sweet natural gas, petroleum naphtha or solar oil.But, along with stock oil becomes heavy, the oily shortage of lightweight material, utilize heavy raw oil to produce low-carbon alkene by the method for catalytic cracking, become a kind of development trend in the refining of petroleum field.As: the disclosed a kind of hydrocarbon conversion processes of producing low-carbon alkene of CN1004878B, the overall yield of propylene and butylene can reach 40 heavy %; The disclosed mink cell focus of CN1218786A is produced the catalytic thermocracking process of ethene and propylene, and ethene and productivity of propylene are all above 18 heavy %; The disclosed a kind of heavy hydrocarbon that utilizes of CN1069016A is to produce ethene, to hold concurrently and produce the hydrocarbon conversion processes of propylene, butylene and light aromatics, and the overall yield of ethene, propylene and butylene can reach 30～40 heavy %.Usually the method that adopts fluid catalytic cracking to produce low-carbon alkene have that reaction steam treatment amount is big, temperature of reaction is high, agent-oil ratio is big, the reaction times is short, characteristics such as gas yield is big in the product, DCC technology for example, cracking severity is big, gas yield has substantially exceeded gas yield in the conventional catalytic cracking process (about about 20 heavy %) in the product more than 50 heavy %.
Reaction product in the conventional catalytic cracking process is separated through following steps: reaction oil gas enters the separation column bottom, is divided into different intermediates in separation column, and cat head is raw gasline and rich gas, and side line has diesel oil and recycle stock, is slurry oil at the bottom of the tower.The gasoline of fractionation cat head and rich gas further are separated into dry gas, liquefied gas and stable gasoline through absorbing-stabilizing system again; Go out device as product after side line diesel oil process stripping, the heat exchange.
Compare with conventional catalytic cracking reaction oil gas, the reaction oil gas of the catalytic cracking process of above-mentioned low-carbon olefines high-output has lighter hydrocarbons content height, oil gas temperature height, the characteristics that water vapour content is high.When adopting conventional catalytic cracking reaction product separation method to separate, because lighter hydrocarbons content height, separation column gas phase load increases, and needs the bigger separation column of designing treatment amount, also increased simultaneously the load of overhead condensation cooling apparatus, reaction oil gas to the pressure drop of pneumatic press ingress increases; Because oil gas temperature height makes that the coking tendency at the bottom of the separation column increases; Because vapour content height in the reaction oil gas, emulsion appears in the material at separation column top easily.
In the reaction product sepn process of ethylene preparing by steam cracker, the Pintsch process gas of pyrolyzer outlet through waste heat boiler reclaim heat after quencher with quenching oil spraying cooling to 220～about 230 ℃, cooled splitting gas enters oil scrubber, cat head sprays with Pyrolysis gas oil PGO, the liquefied gas of cat head enters water wash column, the very useful quenched water of water wash column enters cracking gas compressor after spraying and making tower top temperature be reduced to 40 ℃, water wash column still oil-water mixture separates water outlet and gasoline through water-and-oil separator, as product, another part is delivered to quencher as quenching oil to the liquid phase hydro carbons part that oil wash Tata still is extracted out after the cooling of steam dilution system through overcooling.
The product separation method of above-mentioned traditional ethylene preparing by steam cracker does not consider to contain in the oil gas situation of granules of catalyst, if the granules of catalyst in the oil gas does not add processing, stops up column plate easily.Therefore the sepn process that also is unsuitable for handling high temperature, is rich in lighter hydrocarbons and carries the catalytic cracking reaction oil gas of granules of catalyst.
In sum, be necessary to develop and a kind of the reaction product that is rich in lighter hydrocarbons carried out effective isolating method.
Chinese patent CN1160748A discloses a kind of separation method that is rich in the catalyzed conversion product of propylene, butylene, this method is introduced separation column with crackate, at the bottom of tower, extract recycle stock and slurry oil mixture simultaneously out, its heat is directly made the thermal source of stabilizer tower reboiler, and desorption tower reboiler thermal source is made in the separation column mid-pumparound; After also mid-pumparound and recycle stock and slurry oil mixture can being carried out heat exchange and improving potential temperature, once as the thermal source of stabilizer tower reboiler and desorption tower reboiler.This method still adopts separation column that reaction oil gas is carried out initial gross separation, has solved the reaction oil gas that is rich in propylene, butylene and has separated institute's heat requirement, and reduced the solid content in the slurry oil, has reduced at the bottom of the separation column and the coking of slurry heat-exchanger.
Chinese patent CN1270206A discloses a kind of quench tower of hydro carbons fluidisation catalytic conversion reaction product and has utilized the quick cooling method of this quench tower, be applicable to the chilling of the reactant flow of thermal zone catalyst dust, its quick cooling method is that high-temperature reaction product (600～900 ℃) is contacted cooling with quench liquid in quench tower, temperature is 300～650 ℃ behind the chilling, and the reaction product behind the chilling is introduced product separation and partly separated.
Summary of the invention
The purpose of this invention is to provide a kind of separation method that is suitable for high temperature, is rich in lighter hydrocarbons and carries the catalytic cracking reaction oil gas of catalyst dust.
A kind of catalytic cracking reaction oil and gas separation method that is rich in lighter hydrocarbons, separating step is followed successively by:
(1) pyroreaction oil gas is introduced the quencher bottom, the catalytically cracked material adverse current of introducing with quencher top directly contacts, and at quencher bottom feeding steam, after heat exchange, slurry oil is drawn from the bottom, the catalytically cracked material that has part last running in the reaction oil gas is drawn from side line, and uncooled oil gas is drawn by the quencher top;
(2) the quencher top uncooled oil gas of drawing is introduced the rectifying tower bottom, feed steam in rectifier bottoms, the part gasoline fraction that downstream separation is come out is introduced the top of rectifying tower as refluxing, after rectifying, cat head is drawn gas, diesel oil distillate is extracted in the stage casing out, and the bottom is extracted last running out, and this last running mixes with the catalytically cracked material that the quencher side line is extracted out introduces catalytic cracking unit or hydro-refining unit;
(3) gas of rectifying tower top discharging is introduced water wash column, introduce washing water at the water wash column different sites, after washing, sour water discharging at the bottom of the water wash column is carried the gasoline fraction of a small amount of sour water and is extracted out from the water wash column bottom, and reacted gas ejects material from water wash column;
(4) gasoline fraction that carries a small amount of sour water enters water-and-oil separator and isolates sour water and gasoline fraction, and a part of gasoline fraction is introduced into the rectifying tower top as backflow, and another part is sent to downstream unit and makes with extra care.
The working pressure of the described quencher of separation method provided by the invention is 0.1～0.3MPa, preferred 0.1～0.2MPa, and temperature is 120～500 ℃, preferred 140～380 ℃; The working pressure of rectifying tower is 0.1～0.3MPa, preferred 0.1～0.2MPa, and temperature is 95～250 ℃, preferred 100～180 ℃; The working pressure of water wash column is 0.1～0.3MPa, preferred 0.1～0.2MPa, and temperature is 20～200 ℃, preferred 35～90 ℃;
In the method steps provided by the invention (1),, feed steam in the quencher bottom for preventing coking.Bottom at this quencher is provided with baffle plate, and a part after the slurry oil heat exchange of quencher bottom is circulated to the baffle plate top, and another part slurry oil goes out device; Oil header is set above baffle plate, has the catalytically cracked material of part last running in the reaction oil gas with extraction.
Method provided by the invention is applicable to the separation of the catalytic cracking reaction product of voluminous low-carbon (LC) hydro carbons, also is applicable to the separation of conventional catalytic cracking reaction product.
The manageable reaction oil gas of method provided by the invention contains: the C of 2～30 heavy %
2Following cut, the C of 10～70 heavy %
3～C
4, the C of 10～50 heavy %
5And gasoline, the diesel oil of 3～30 heavy %, the slurry oil of 0～20 heavy %.Preferred reaction oil gas consists of and contains: the C of 10～30 heavy %
2Following cut, the C of 40～60 heavy %
3～C
4, the C of 10～20 heavy %
5And gasoline, the diesel oil of 3～10 heavy %, the slurry oil of 1～5 heavy %.
The advantage of method provided by the invention is:
1. reaction oil gas and catalytically cracked material direct contact heat-exchanging in quencher, the heat exchange efficiency height makes reaction oil gas cooling rapidly in a short period of time, has improved the temperature of catalytically cracked material simultaneously;
2. compare with conventional catalytic cracking separation method, reduced the cooling load on main fractionating tower top, reduced the pressure drop of reaction oil gas, help improving the inlet pressure of pneumatic press, thereby reduced the energy consumption of pneumatic press to the pneumatic press inlet;
3. because the aromatic hydrocarbons and the diolefine that contain in the reaction product slurry oil are diluted, cooling rapidly in water cooler has simultaneously reduced water cooler and rectifying tower bottom coke, and has eliminated the emulsion of the material on separation column top;
4. the little amount of catalyst dust of carrying secretly in the reaction oil gas can be washed down, and draws from anti-quencher bottom in company with slurry oil.
Description of drawings
Fig. 1 is the schematic flow sheet of method provided by the invention;
Wherein: the 1-quencher; The 2-rectifying tower; The 3-water wash column; The 4-water-and-oil separator; The 5-mixing tank; 6～25-pipeline.
Embodiment
Below in conjunction with accompanying drawing method provided by the invention is described further.
Contain the bottom of the high-temperature oil gas of catalyst dust through pipeline 7 introducing quenchers 1, catalytically cracked material is through the top of pipeline 8 introducing quenchers 1, the two adverse current directly contacts, catalytically cracked material is heated in the process that flows downward, the reaction oil gas condensation that in the process that rises, constantly is cooled, for preventing coking, feed steam from quencher 1 bottom through pipeline 9.The slurry oil that is entrained with catalyst dust is extracted out from quencher 1 bottom through pipeline 11; Uncooled reaction oil gas (containing the following cut of diesel oil) is drawn through pipeline 12 in top at this quencher; Extract the catalytically cracked material that has reaction oil gas last running through pipeline 10 out from the oil header that is arranged in the baffle plate top.
The oil gas of extracting out from quencher 1 top enters rectifying tower 2 through pipeline 12 from the bottom, feed stripped vapor in rectifying tower 2 bottoms through pipeline 13, a part of gasoline fraction that water-and-oil separator 4 is separated is as the top of refluxing and introducing rectifying tower 2 through pipeline 14 simultaneously, the gas that contains gasoline fraction is drawn at top at rectifying tower 2 through pipeline 18, stage casing at rectifying tower 2 is extracted diesel oil distillate out through pipeline 15, extract last running in rectifying tower 2 bottoms out through pipeline 16, last running mixes after pipeline 17 is delivered to catalyst cracker or hydro-refining unit at mixing tank 5 with the catalytically cracked material that quencher 1 is extracted out.
The gas that draw at rectifying tower 2 tops enters water wash column 3 through pipeline 18, washing water is introduced through pipeline 19,20 in top at water wash column 3 from different positions, under the effect of washing water, gas is cooled, most of gasoline fraction is wherein washed, extract most of sour water from the bottom of water wash column 3 out through pipeline 21, carry gasoline fraction the extracting out of a small amount of sour water from water wash column 3 bottoms through pipeline 23, the reacted gas that carries the part gasoline fraction is extracted out from the rectifying tower top through pipeline 22, and is sent to downstream unit and separates.
Carrying the gasoline fraction of a small amount of sour water introduces in the water-and-oil separator 4 through pipeline 23, after oily water separation, sour water is drawn through pipeline 25, gasoline fraction is drawn through pipeline 24, wherein a part is incorporated into rectifying tower 2 tops as backflow through pipeline 14, and another part is sent to downstream unit through pipeline 6 and makes with extra care.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Embodiment
See Table 1 from the composition of the next pyroreaction oil gas that carries the little amount of catalyst dust of catalytic cracking unit, adopt method provided by the invention that it is separated, technical process as shown in Figure 1, the character of the catalytically cracked material that comes from the irrigated area sees Table 2, the operational condition of quencher, rectifying tower and water wash column sees Table 3 in the sepn process, and raw material properties and composition after the raw gasline that obtains after the separation, solar oil, slurry oil and the heat exchange are listed in table 4.
Table 1
| Catalytic cracking reaction oil gas | |
| Temperature, ℃ pressure, MPa flow, kg/h | 620 0.17 202221 |
| Form heavy %H 2 N 2 O 2 H 2O CO CO 2 H 2S CH 4 C 2H 6 C 2H 4 C 3H 8 C 3H 6 n-C 4H 10 i-C 4H 10 C 4H 8-1 iC 4H 8 c-C 4H 8-2 t-C 4H 8-2 C 5 +The gasoline, diesel slurry oil | 0.31?0.70?0.08?29.670.00?0.20?0.29?5.01?2.84?9.80?2.07?21.630.54?1.20?2.02?4.36?1.87?2.57?10.513.09?1.24? |
Table 2
| Temperature, ℃ flow, kg/h proportion, g/cm
3Boiling range, ℃ |
80 1500000.8951 323 378 399 463 547 |
Table 3
| Quencher | Rectifying tower | Water wash column | |
| Head temperature, ℃ bottom temp, ℃ top pressure, MPa | 168?360?0.16 | 108?160?0.15 | 40 80 0.14 |
Table 4
| Gasoline fraction | Diesel oil distillate | Slurry oil | Raw material after the heat exchange | |
| Temperature, ℃ proportion, g/cm
3Boiling range, ℃ |
0.74 44 85 112?126?141?163?183? | 0.985 229 256 274 292 320 357 360 | 1.1 368405438475526560- | 250?0.99 305?389?455?539?- -- |
As can be seen from Table 4, temperature is that to enter quencher and temperature be that 80 ℃ catalytically cracked material directly contacts chilling to 620 ℃ reaction oil gas, the temperature of catalytically cracked material is brought up to 250 ℃, the following cut of diesel oil is cooled to 168 ℃, again after the rectifying tower cooling, the following cut of gasoline is drawn with 108 ℃ temperature, in water wash column internal cooling to 40～80 ℃.
Claims (4)
1. separation method that is rich in the catalytic cracking reaction oil gas of lighter hydrocarbons is characterized in that separating step is followed successively by:
(1) pyroreaction oil gas is introduced the quencher bottom, the catalytically cracked material adverse current of introducing with quencher top directly contacts, and at quencher bottom feeding steam, after heat exchange, slurry oil is drawn from the bottom, the catalytically cracked material that has part last running in the reaction oil gas is drawn from side line, and uncooled oil gas is drawn by the quencher top;
(2) the quencher top uncooled oil gas of drawing is introduced the rectifying tower bottom, feed steam in rectifier bottoms, the part gasoline fraction that downstream separation is come out is introduced the top of rectifying tower as refluxing, after rectifying, cat head is drawn gas, diesel oil distillate is extracted in the stage casing out, and the bottom is extracted last running out, and this last running mixes with the catalytically cracked material that the quencher side line is extracted out introduces catalytic cracking unit or hydro-refining unit;
(3) gas of rectifying tower top discharging is introduced water wash column, introduce washing water at the water wash column different sites, after washing, sour water discharging at the bottom of the water wash column is carried the gasoline fraction of a small amount of sour water and is extracted out from the water wash column bottom, and reacted gas ejects material from water wash column;
(4) gasoline fraction that carries a small amount of sour water enters water-and-oil separator and isolates sour water and gasoline fraction, and a part of gasoline fraction is introduced into the rectifying tower top as backflow, and another part is sent to downstream unit and makes with extra care;
Wherein, described reaction oil gas contains: the C of 2～30 heavy %
2Following cut, the C of 10～70 heavy %
3～C
4Hydrocarbon, the C of 10～50 heavy %
5And gasoline, the diesel oil of 3～30 heavy %, the slurry oil of 0～20 heavy %.
2. according to the method for claim 1, the working pressure that it is characterized in that described quencher is 0.1～0.3MPa, and temperature is 120～500 ℃; The working pressure of rectifying tower is 0.1～0.3MPa, and temperature is 95～250 ℃; The working pressure of water wash column is 0.1～0.3MPa, and temperature is 20～200 ℃.
3. according to the method for claim 2, the working pressure that it is characterized in that described quencher is 0.1～0.2MPa, and temperature is 140～380 ℃; The working pressure of rectifying tower is 0.1～0.2MPa, and temperature is 100～180 ℃; The working pressure of water wash column is 0.1～0.2MPa, and the temperature at top is 35～90 ℃.
4. according to the method for claim 1, it is characterized in that described reaction oil gas contains: the C of 10～30 heavy %
2Following cut, the C of 40～60 heavy %
3～C
4Hydrocarbon, the C of 10～20 heavy %
5And gasoline, the diesel oil of 3～10 heavy %, the slurry oil of 1～5 heavy %.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006100869741A CN101092570B (en) | 2006-06-22 | 2006-06-22 | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006100869741A CN101092570B (en) | 2006-06-22 | 2006-06-22 | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101092570A CN101092570A (en) | 2007-12-26 |
| CN101092570B true CN101092570B (en) | 2011-04-20 |
Family
ID=38991014
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2006100869741A Active CN101092570B (en) | 2006-06-22 | 2006-06-22 | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101092570B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8273936B2 (en) * | 2010-11-22 | 2012-09-25 | Equistar Chemicals, Lp | Process for cracking heavy hydrocarbon feed |
| 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 |
| CN102925213B (en) * | 2011-08-09 | 2015-01-07 | 中国石油化工股份有限公司 | Treatment method for light hydrocarbon-containing petrochemical industry gas |
| CN103087765B (en) * | 2011-10-28 | 2015-09-16 | 中国石油化工股份有限公司 | A kind of production method of low-carbon alkene |
| CN102911737A (en) * | 2012-10-08 | 2013-02-06 | 沈阳石蜡化工有限公司 | Method for coupling oil refining and chemical processes |
| CN103910595B (en) * | 2013-01-06 | 2015-07-15 | 中石化上海工程有限公司 | Separation method for mixture system containing C2, C3, C4, C5 and heavy components |
| CN109355087B (en) * | 2018-11-21 | 2021-01-15 | 陕西延长石油（集团）有限责任公司 | Step recovery device and method for oil product in gas containing oil dust |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1782023A (en) * | 2004-11-30 | 2006-06-07 | 中国石油化工股份有限公司 | Separating method for hydrocarbon oil catalytic cracking reaction products |
-
2006
- 2006-06-22 CN CN2006100869741A patent/CN101092570B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1782023A (en) * | 2004-11-30 | 2006-06-07 | 中国石油化工股份有限公司 | Separating method for hydrocarbon oil catalytic cracking reaction products |
Non-Patent Citations (1)
| Title |
|---|
| JP昭61-164618A 1986.07.25 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101092570A (en) | 2007-12-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| KR20100097092A (en) | Splitter with multi-stage heat pump compressor and inter-reboiler | |
| CN104230617B (en) | The method that MTO technique couples with Petroleum and Deposition During Propane Pyrolysis order separating technology | |
| CN1793092A (en) | Recovery and purification of ethylene | |
| CN102304009B (en) | Method and system for separating MTP (Methanol to Propylene) reaction mixed gas | |
| CN108276236B (en) | Cryogenic separation and recovery method for Fischer-Tropsch synthesis tail gas for increasing olefin yield | |
| CN110591751A (en) | Improved process of light hydrocarbon recovery technology | |
| CN202081036U (en) | Mixed gas separating system in MTP reaction | |
| CN109809957A (en) | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique | |
| CN101323798A (en) | Catalytic conversion method and special apparatus therefor | |
| CN101381617A (en) | Fractionation method of hydrocarbon mixtures | |
| CN101270304B (en) | Fine purification technique for coke oven gas | |
| CN110527555A (en) | A kind of system of long distillate cracking of crude oil ethylene | |
| CN112410069B (en) | Hydrorefining process for catalytic cracking crude gasoline | |
| CN104926584B (en) | A kind of system and method preparing iso-butane | |
| CN112830861B (en) | Device and method for producing n-butane | |
| CN108587684A (en) | A kind of joint aromatics production line CONTINUOUS REFORMER unit | |
| CN100378195C (en) | Separating method for hydrocarbon oil catalytic cracking reaction products | |
| CN209193845U (en) | Separating device for methanol-to-olefin gas | |
| CN111320525A (en) | Non-low temperature separation process for ethylene-rich catalytic cracking gas | |
| CN109734549A (en) | Naphtha and Deposition During Propane Pyrolysis sequentially separate the method coupled with PDH | |
| CN111533633B (en) | Catalytic cracking process | |
| CN111747814B (en) | Method for coupling deethanization process and propane dehydrogenation process before hydrocarbon steam cracking | |
| CN111848327B (en) | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking | |
| CN110760334B (en) | Deep processing method of catalytic slurry oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |