CN113355131B - Multi-working-condition operation device and method for decarbonization nine towers of pyrolysis gasoline hydrogenation device - Google Patents
Multi-working-condition operation device and method for decarbonization nine towers of pyrolysis gasoline hydrogenation device Download PDFInfo
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- CN113355131B CN113355131B CN202010149131.1A CN202010149131A CN113355131B CN 113355131 B CN113355131 B CN 113355131B CN 202010149131 A CN202010149131 A CN 202010149131A CN 113355131 B CN113355131 B CN 113355131B
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
Abstract
The invention belongs to the technical field of pyrolysis gasoline hydrogenation, and discloses a device and a method for multi-working-condition operation of a nine decarbonization tower of a pyrolysis gasoline hydrogenation device, wherein the device comprises the nine decarbonization tower, a tower top extraction pipeline connected with a hydrogenation reaction system is arranged at the tower top of the nine decarbonization tower, and a tower top condenser, a reflux tank and a tower top pump are sequentially arranged on the tower top extraction pipeline; a carbon eight-side line extraction pipeline and a side line extraction gas phase balance port are arranged at the middle lower part of the decarbonization nine tower, and a carbon eight-side line extraction flow control assembly, a mixer, a carbon eight-product tank, a carbon eight-product pump, a carbon eight-product cooler and a discharge valve are sequentially arranged on the carbon eight-side line extraction pipeline; the bottom of the nine decarbonizing towers is provided with tower kettle extraction pipelines, tower kettle pumps and nine carbon product coolers are sequentially arranged on the tower kettle extraction pipelines, and the bottoms of the nine decarbonizing towers are provided with reboilers. The device and the method of the invention can be suitable for the operation under two working conditions, can meet the requirement of the change of the product scheme from the overall planning, and can save energy to the maximum extent.
Description
Technical Field
The invention belongs to the technical field of pyrolysis gasoline hydrogenation, and particularly relates to a device and a method for multi-working-condition operation of a decarbonization nine-tower of a pyrolysis gasoline hydrogenation device.
Background
The pyrolysis gasoline is a byproduct for preparing ethylene by steam pyrolysis, mainly comprises C5-C9+ fraction, and a C5-product, a C6-C8 hydrogenated gasoline and a C9+ product can be obtained after crude pyrolysis gasoline from an ethylene device is separated and hydrogenated by a pyrolysis gasoline hydrogenation device. C5-and C9+ are sold as products, and C6-C8 center fraction hydrogenated gasoline is sent to a downstream aromatic extraction device for further separation. In recent years, as the demand for styrene increases, the added value of styrene in raw pyrolysis gasoline increases more and more, and many factories are equipped with styrene extraction devices to extract styrene in raw pyrolysis gasoline. In order to meet the requirements of a downstream styrene extraction device, a nine decarbonization tower is set as an eight decarbonization tower, C6-C7 fractions are extracted from the top of the tower, C8+ fractions are extracted from the bottom of the tower, the C8+ fractions are sent to the styrene extraction device for further treatment to obtain qualified styrene products, and raffinate oil is returned to the pyrolysis gasoline hydrogenation device for hydrogenation.
Because styrene is easy to polymerize, the overhaul period of the styrene extraction device is short, and the shutdown overhaul is needed once in about 2 years. When a styrene device is stopped for maintenance, a plurality of factories hope that C9+ can be extracted from the decarbonization nine-tower kettle of a pyrolysis gasoline hydrogenation device, and the C8 fraction rich in styrene is extracted from the tower top and directly subjected to hydrogenation treatment and is not sent to a styrene extraction device. Under the condition, the decarbonization nine tower is required to meet the requirements of two operation working conditions, the working conditions that C6-C7 fractions are extracted from the top of the tower and C8+ fractions are extracted from the bottom of the tower when the styrene extraction device is in normal operation can be met, and the working conditions that C6-C8 fractions are extracted from the top of the tower and C9+ fractions are extracted from the bottom of the tower when the styrene extraction device is stopped can also be met.
In view of the above needs in the prior art, it is urgently needed to provide a device for decarbonization nine-tower multi-operating-condition operation of a pyrolysis gasoline hydrogenation device, which is better suitable for the needs of actual production.
Disclosure of Invention
In view of the above situation, the present invention aims to provide a device and a method for multi-operating conditions of a nine-tower decarbonization unit of a pyrolysis gasoline hydrogenation unit, which can select corresponding operating conditions according to the production conditions of downstream devices and market changes, and can meet the requirements of product scheme changes in the overall planning and save energy to the maximum extent.
The invention provides a device for multi-working-condition operation of a nine-tower decarburization device of a pyrolysis gasoline hydrogenation device, which comprises a nine-tower decarburization device, wherein a first feed inlet and a second feed inlet are arranged in the middle of the nine-tower decarburization device, and the first feed inlet is positioned above the second feed inlet;
the top of the nine decarburization towers is provided with a top extraction pipeline connected with a hydrogenation reaction system, and along the material flow direction, the top extraction pipeline is sequentially provided with a top condenser, a reflux tank and a top pump, the reflux tank is connected with a vacuum pumping system through a nine decarburization tower tail gas condenser, and the top extraction pipeline at the downstream of the top pump is provided with a reflux pipeline connected with the upper part of the nine decarburization towers;
a carbon eight-side line extraction pipeline and a side line extraction gas phase balance port are arranged at the middle lower part of the nine decarburization towers, a carbon eight-side line extraction quantity control assembly, a mixer, a carbon eight-product tank, a carbon eight-product pump, a carbon eight-product cooler and a discharge valve are sequentially arranged on the carbon eight-side line extraction pipeline along the material flow direction, a return pipeline connected with the mixer is arranged on the carbon eight-side line extraction pipeline between the carbon eight-product cooler and the discharge valve, a cooling carbon eight-return quantity control assembly is arranged on the return pipeline, and the top of the carbon eight-product tank is connected with the side line extraction gas phase balance port through a gas phase balance line;
the bottom of nine towers of decarbonization is equipped with tower cauldron and draws the pipeline, along the material flow direction, is equipped with tower cauldron pump and nine carbon product coolers on the tower cauldron production pipeline in proper order, the bottom of nine towers of decarbonization is equipped with the reboiler.
The second aspect of the invention provides a method for carrying out multi-working-condition operation of a nine-tower decarburization device of a pyrolysis gasoline hydrogenation device by adopting the device, which comprises the following steps:
the working condition I is as follows: the raw material from the five decarburization tower system enters a nine decarburization tower through a first feeding hole, and C6-C7 fractions are extracted from an extraction pipeline at the top of the tower; c8 fraction is extracted from a carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower kettle extraction pipeline;
and a second working condition: the raw material from the five decarbonization tower system enters a nine decarbonization tower through a second feeding hole, and C6-C8 fractions are extracted from an overhead extraction pipeline; closing the carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower bottom extraction pipeline.
The device and the method for the decarbonization nine-tower multi-working-condition operation of the pyrolysis gasoline hydrogenation device have the following characteristics and advantages:
(1) The device and the method for the decarbonization nine-tower multi-working-condition operation of the pyrolysis gasoline hydrogenation device can meet the requirement of changing the product scheme caused by market demand change or starting and stopping of a downstream device.
(2) The device of the invention adopts a tower system to meet the change of different product schemes, saves energy and reduces the total investment.
(3) The nine decarbonizing tower internals adopt the mode of combining the filler and the tower plate, thus not only reducing the pressure drop of the whole tower, but also avoiding the blockage of the tower internals caused by the polymerization of unsaturated hydrocarbon at high temperature; the pressure drop of the whole tower is reduced, so that the pressure of the tower kettle is reduced, the temperature is reduced, the steam consumption is reduced, and the decomposition of heavy components in the tower kettle is reduced.
(4) According to the carbon eight-side-line extraction system, the extraction amount is controlled by the carbon eight-side-line extraction amount control assembly, so that the automation degree is high, and the product quality is more reliable.
(5) According to the carbon eight-side-draw system provided by the invention, the cooled C8 product and the side-draw hot material are directly mixed for cooling, so that the polymerization risk caused by high temperature can be simply and conveniently avoided.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without limiting the invention.
FIG. 1 is a schematic process flow diagram of a nine-tower multi-operating-condition decarbonization apparatus of a pyrolysis gasoline hydrogenation apparatus according to an embodiment of the present invention.
Description of the reference numerals
Equipment: 1, a nine-tower decarburization; 2, a mixer; a 3-carbon eight-product tank; a 4-carbon eight-product pump; a 5-carbon eight-product cooler; 6, a tower top condenser; 7, a reflux tank; 8, a tower top pump; 9, a nine-tower tail gas decarbonizer; 10 a reboiler; 11 tower kettle pump; a 12 carbon nine product cooler; 13 a discharge valve; 14 a first thermometer; 15 a first flow meter; 16 a first regulating valve; 17 a second thermometer; 18 a second flow meter; 19 a second regulating valve; an RS hydrogenation reaction system; a VS vacuum pumping system; a TS decarburization five-tower system;
logistics: s-1, feeding under a nine-tower working condition; s-2, feeding under nine working conditions of decarburization; s-3, extracting a product from the top of the nine decarbonization towers; s-4 C8 product; s-5 C9+ product.
Detailed Description
In order that the present invention may be more readily understood, the present invention will now be described in detail with reference to the following examples and the accompanying drawings, which are given by way of illustration only and are not intended to limit the invention.
According to a first aspect of the invention, the invention provides a device for carrying out multi-working-condition operation on a nine-tower decarburization device of a pyrolysis gasoline hydrogenation device, which comprises a nine-tower decarburization device, wherein a first feed inlet and a second feed inlet are arranged in the middle of the nine-tower decarburization device, and the first feed inlet is positioned above the second feed inlet;
the top of the nine decarbonizing towers is provided with a tower top extraction pipeline connected with a hydrogenation reaction system, and along the material flow direction, the tower top extraction pipeline is sequentially provided with a tower top condenser, a reflux tank and a tower top pump, the reflux tank is connected with a vacuum-pumping system through a nine decarbonizing tower tail gas condenser, and the tower top extraction pipeline at the downstream of the tower top pump is provided with a reflux pipeline connected with the upper part of the nine decarbonizing towers;
a carbon eight-side line extraction pipeline and a side line extraction gas phase balance port are arranged at the middle lower part of the nine decarburization tower, a carbon eight-side line extraction control assembly, a mixer, a carbon eight-product tank, a carbon eight-product pump, a carbon eight-product cooler and a discharge valve are sequentially arranged on the carbon eight-side line extraction pipeline along the material flow direction, a return pipeline connected with the mixer is arranged on the carbon eight-side line extraction pipeline between the carbon eight-product cooler and the discharge valve, a cooling carbon eight-return control assembly is arranged on the return pipeline, and the top of the carbon eight-product tank is connected with the side line extraction gas phase balance port through a gas phase balance line;
the bottom of nine towers of decarbonization is equipped with tower cauldron and draws the pipeline, along the material flow direction, is equipped with tower cauldron pump and nine product coolers of carbon on the tower cauldron production pipeline in proper order, the bottom of nine towers of decarbonization is equipped with the reboiler. In the invention, the tower internals of the nine decarburization towers comprise upper packing and tower plates arranged below the packing. A first feeding hole and a second feeding hole are formed in the nine decarburization tower, so that the separation requirements of a first working condition and a second working condition are met respectively, and different feeding holes are correspondingly switched under different operating conditions. Preferably, the first feed inlet is arranged between the packing and the tower plate, and the second feed inlet is arranged at the upper part of the tower plate.
Preferably, the carbon eight-side draw-out flow control assembly comprises a first thermometer, a first flowmeter and a first regulating valve, wherein the first thermometer and the first regulating valve are arranged on the carbon eight-side draw-out line, the first thermometer is arranged at the upper part of the tower plate, and the first regulating valve is controlled in series through the first thermometer and the first flowmeter.
According to the invention, the height of the packing layer and the number of the trays of the column internals can be suitably adjusted according to the properties of the raw materials and the product index. Preferably, the height of the packing is 4 to 6m, and the number of the trays is 33 to 55 pieces.
Preferably, the second feed inlet is arranged at the 10 +/-3 th tower plate counted from top to bottom.
In the invention, the top (gas phase space) of the carbon eight-product tank is connected with the side line extraction gas phase balance port through a gas phase balance line, so that the pressure of the side line extraction gas phase balance port is kept consistent, and the extracted product automatically flows into the carbon eight-product tank.
Preferably, the carbon eight-sidedraw line and the sidedraw gas phase equalizing port are located at the 12 + 3 trays.
According to the invention, the carbon eight-side draw is controlled by the carbon eight-side draw control assembly, wherein the opening of the first regulating valve is controlled by the temperature of the first thermometer. Preferably, the first thermometer is arranged at the 2 nd to 6 th tray (sensitive plate).
Preferably, the cooling carbon eight-return quantity control assembly comprises a second thermometer, a second flowmeter and a second regulating valve, the second thermometer and the second regulating valve are arranged on the return pipeline, the second thermometer is arranged at the outlet of the carbon eight-product tank, and the second regulating valve is controlled in series through the second thermometer and the second flowmeter. The return amount of the carbon eight cooled product is controlled by the outlet temperature of the carbon eight product tank. Preferably, the carbon eight product tank outlet temperature is less than 75 ℃.
According to the invention, the decarbonization nine-tower tail gas condenser can be cooled by adopting propylene refrigerant.
Preferably, the reboiler has two stages, one stage being on stream and the other stage being on standby, and the reboiler is heated using a 1.3mpa g steam heat source.
Components of the system which are not limited in the invention can be selected conventionally according to the prior art, and belong to the conventional technical means.
According to a second aspect of the invention, the invention provides a method for carrying out multi-working-condition operation of a nine-tower decarburization device of a pyrolysis gasoline hydrogenation device by adopting the device, which comprises the following steps:
the working condition I is as follows: the raw material from the five decarbonization tower system enters a nine decarbonization tower through a first feeding hole, and C6-C7 fractions are extracted from an overhead extraction pipeline; c8 fraction is extracted from a carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower kettle extraction pipeline;
and a second working condition: the raw material from the five decarbonization tower system enters a nine decarbonization tower through a second feeding hole, and C6-C8 fractions are extracted from an overhead extraction pipeline; closing the carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower bottom extraction pipeline.
According to the invention, the operating flexibility of the decarbonization nine column can be 60% -110% under the working conditions. The operating parameters of the nine decarbonizing towers are adjusted as required to meet the requirements of the tower top, the side line and the tower kettle.
The operation temperature of the nine decarbonization towers can be 53-140 ℃, preferably 53-135 ℃, specifically, the operation temperature of the top of the tower is 53 ℃, the temperature of the bottom of the tower is 135 ℃, and the temperature of the side draw is 105 ℃.
The operation pressure of the nine decarbonization towers is negative pressure, and the system is pumped by a tower top vacuum pump to form negative pressure, preferably-0.073 to-0.049 MpaG. Preferably, the overhead operating pressure is from 20 to 40KPaA.
The amount of the carbon eight-side-line extracted product is controlled according to the temperature of the side-line extracted sensitive plate, the extracted product automatically flows into a carbon eight-product tank, and is mixed with a carbon eight-cooling product through a mixer before entering the carbon eight-product tank, so that the temperature is reduced to be below 75 ℃. And the liquid phase discharged material of the carbon eight product tank is boosted by a carbon eight product pump, and is cooled to 43 ℃ by a carbon eight product cooler, and then a part of the liquid phase discharged material returns to the inlet mixer of the carbon eight product tank, and the rest of the liquid phase discharged material is sent out. The return of the carbon eight cooled product is controlled by the carbon eight product tank outlet temperature, which is preferably no greater than 75 ℃.
According to the invention, under the working condition two, the operational flexibility of the nine decarburization towers is 60% -100%. The operating parameters of the nine decarbonizing towers are adjusted as required to meet the product requirements of the tower top and the tower kettle.
The operation temperature of the nine decarburization towers can be 67-140 ℃, preferably 67-134 ℃, specifically, the operation temperature of the top of the tower is 67 ℃, and the operation temperature of the bottom of the tower is 134 ℃.
The operation pressure of the nine decarbonization towers is negative pressure, and the system is pumped by a tower top vacuum pump to form negative pressure, preferably-0.073 to-0.049 MpaG. Preferably, the overhead operating pressure is from 20 to 40KPaA.
The device and the method of the invention can meet the requirements of two separation working conditions: when the downstream styrene extraction device is in normal production or the market condition of styrene is good, C6-C7 fractions are extracted from the top of the nine-tower decarburization tower, C8 fractions are extracted from the side line, C9+ fractions are extracted from the bottom of the tower, and the C8 fractions extracted from the side line are sent to the downstream styrene extraction device; when the downstream styrene device is stopped or the market condition of styrene is poor, the decarbonization nine tower can be switched to another operating condition, C6-C8 fractions are extracted from the tower top, C9+ fractions are extracted from the tower bottom, and no side line is extracted.
The process parameters which are not limited in the invention can be set conventionally according to the prior art.
The present invention will be described in detail by way of examples.
Examples
This example is provided to illustrate the device and method of the present invention for multi-operating decarbonization nine-tower system for a pyrolysis gasoline hydrogenation unit.
As shown in figure 1, the invention provides a device for a nine-tower multi-working-condition operation of a pyrolysis gasoline hydrogenation device, which comprises a nine-tower decarburization 1, wherein a first feed inlet and a second feed inlet are arranged in the middle of the nine-tower decarburization 1, and the first feed inlet is positioned above the second feed inlet;
the top of the nine decarburization towers 1 is provided with a top extraction pipeline connected with a hydrogenation reaction system RS, along the material flow direction, the top extraction pipeline is sequentially provided with a top condenser 6, a reflux tank 7 and a top pump 8, the reflux tank 7 is connected with a vacuum-pumping system VS through a tail gas condenser 9 of the nine decarburization towers, and the top extraction pipeline at the downstream of the top pump 8 is provided with a reflux pipeline connected with the upper part of the nine decarburization towers 1;
a carbon eight-side line extraction pipeline and a side line extraction gas phase balance port (not shown) are arranged at the middle lower part of the decarbonization nine tower 1, a carbon eight-side line extraction control assembly, a mixer 2, a carbon eight-product tank 3, a carbon eight-product pump 4, a carbon eight-product cooler 5 and a discharge valve 13 are sequentially arranged on the carbon eight-side line extraction pipeline along the material flow direction, a return pipeline connected with the mixer 2 is arranged on the carbon eight-side line extraction pipeline between the carbon eight-product cooler 5 and the discharge valve 13, a cooling carbon eight-return control assembly is arranged on the return pipeline, and the top of the carbon eight-product tank 3 is connected with the side line extraction gas phase balance port through a gas phase balance line;
the bottom of the nine decarbonization tower 1 is provided with a tower kettle extraction pipeline, a tower kettle pump 11 and a nine carbon product cooler 12 are sequentially arranged on the tower kettle extraction pipeline along the material flow direction, and the bottom of the nine decarbonization tower 1 is provided with a reboiler 10.
The tower internals of the nine decarbonization tower 1 comprise an upper filler and a tower plate arranged below the filler; the first feed inlet is arranged between the filler and the tower plate, and the second feed inlet is arranged at the upper part of the tower plate.
The carbon eight-side draw flow control assembly comprises a first thermometer 14, a first flowmeter 15 and a first regulating valve 16, wherein the first flowmeter 14 and the first regulating valve 16 are arranged on the carbon eight-side draw line, the first thermometer 14 is arranged at the upper part of a tower plate, and the first regulating valve 16 is controlled in series through the first thermometer 14 and the first flowmeter 15.
The height of the filler is 5m, and the number of the tower plates is 46; counting from top to bottom, wherein the second feed inlet is arranged at the 10 th tower plate; the carbon eight-side-draw pipeline and the side-draw gas phase balance port are arranged at the 12 th tower plate; the first thermometer is arranged at the 5 th tower plate.
The cooling carbon eight-return-amount control assembly comprises a second thermometer 17, a second flowmeter 18 and a second regulating valve 19, wherein the second thermometer 18 and the second regulating valve 19 are arranged on a return pipeline, the second thermometer 17 is arranged at a liquid phase outlet of the carbon eight-product tank 3, and the second regulating valve 19 is controlled in series through the second thermometer 17 and the second flowmeter 18.
The tail gas condenser 9 of the nine decarbonization towers is cooled by a propylene refrigerant.
The reboiler was provided in two, one operating and the other standby (not shown), and the reboiler was heated using a 1.3MPaG steam heat source.
The composition of the crude pyrolysis gasoline feed to a pyrolysis gasoline hydrogenation unit is shown in table 1 below.
The crude pyrolysis gasoline feed flow rate was 17t/h.
TABLE 1
| Components | Composition (wt%) | Components | Composition (wt%) | Components | Composition (wt%) |
| Propane | 0.004 | 14 hexadiene | 0.045 | Cyclooctadiene | 0.048 |
| 1, 3-butadiene | 0.293 | 14 Cyclohexanediene | 2.714 | Indene | 0.02 |
| Butene-1 | 0.091 | Toluene | 11.701 | Indanes | 0.02 |
| Butane | 0.291 | Heptane as a substitute for petroleum jelly | 0.589 | Isopropyl benzene | 0.009 |
| Cyclopentane | 3.108 | Cycloheptane | 0.742 | Methyl styrene | 0.347 |
| Isopentane | 3.804 | Heptene | 0.774 | 1 |
0.537 |
| Pentane (pentane) | 1.97 | Cycloheptene | 0.192 | Nonene | 0.131 |
| Cyclo-pentene | 0.511 | 2 methyl 24 hexadiene | 0.628 | Nonane | 2.671 |
| |
0.551 | Styrene (meth) acrylic acid ester | 4.393 | Ring C9 | 0.038 |
| Pentene 2 | 0.475 | Ethylbenzene production | 2.828 | Decene | 0.2 |
| 1, 3-cyclopentadiene | 4.181 | Ortho-xylene | 1.139 | Decane | 0.3 |
| Isoprene (I) | 2.096 | Meta-xylene | 2.218 | Naphthalene | 0.16 |
| 1, 3-pentadiene | 0.339 | Para xylene | 1.457 | Butylene benzene | 0.3 |
| Benzene and its derivatives | 36.776 | Octane | 0.467 | Isobutyl benzene | 0.5 |
| Hexane (C) | 0.916 | Cyclooctane | 0.443 | Dicyclopentadiene | 3.986 |
| Cyclohexane | 2.428 | Octene, its production and use | 0.129 | Thiophene(s) | 0.03 |
| Hexene | 1.623 | Cyclooctene | 0.708 | Total up to | 100％ |
| Cyclohexene | 0.049 | Dimethylhexadiene | 0.033 |
By adopting the device, the specific operation steps under two working conditions are as follows:
1. the nine decarbonizing towers 1 are operated under the working condition I (namely C6-C7 fractions are extracted from the top of the tower, C8 fractions are extracted from the side line, and C9+ fractions are extracted from the bottom of the tower).
And (3) opening a feeding root valve (a first feeding port valve) under the first working condition of the decarbonization nine tower 1, and closing a feeding root valve (a second feeding port valve) under the second working condition. After the crude pyrolysis gasoline is subjected to C5-fraction separation by a five-tower decarbonization system TS, the C6+ fraction enters a nine-tower decarbonization 1 by pressure difference, and the nine-tower decarbonization 1 is subjected to one-working-condition operation. The working conditions of the nine decarbonizing tower 1 are shown in Table 2. C6-C7 fractions are extracted from the tower top and sent to a hydrogenation reaction system RS, C9+ fractions are extracted from the tower bottom and sent to the outside, and C8 products are extracted from the side line. The C8 product extraction amount is adjusted according to the temperature of the sensitive plate, and the C8 product is mixed with the returned cooling material and enters the C8 product tank 3 after being cooled. Then the mixture is pressurized and cooled and sent out of the house. The cooling C8 return is adjusted based on the C8 product tank 3 outlet temperature. The specification of each product under the first operating condition is shown in table 3.
2. And (3) operating the nine decarburization towers 1 under the working condition II (namely, C6-C8 fractions are extracted from the tops of the towers, C9+ fractions are extracted from the bottoms of the towers, and no side stream is extracted).
A feeding root valve (a second feeding port valve) of the working condition two of the decarburizing nine tower 1 is opened, a feeding root valve (a first feeding port valve) of the working condition one is closed, and a carbon eight-side line extraction pipeline root valve is closed. After the crude pyrolysis gasoline is subjected to C5-fraction separation by a five-tower decarbonization system TS, the C6+ fraction enters a nine-tower decarbonization 1 by pressure difference, and the nine-tower decarbonization 1 is subjected to a second working condition operation. The operating conditions of the working conditions of the nine decarbonizing towers 1 are shown in the table 2. C6-C8 fractions are extracted from the tower top and sent to a reaction system, and C9+ fractions are extracted from the tower bottom and sent to the outside. The specifications of the products under the second working condition are shown in a table 4.
TABLE 2
TABLE 3
| Item | Make up of | Specification of | Flow/kg/h |
| Tower top | C6-C7 fraction | Styrene is less than or equal to 0.5wt percent | 10253 |
| Tower kettle | C9+ fraction | C8 aromatic hydrocarbon is less than or equal to 5wt% | 1068 |
| Side line | C8 fraction | Toluene is less than or equal to 1wt percent | 2723 |
TABLE 4
| Item | Composition of | Specification of | Flow/kg/h |
| Tower top | C6-C8 fraction | C9 aromatic hydrocarbon is less than or equal to 1wt% | 12588 |
| Tower kettle | C9+ fraction | Less than or equal to 3 weight percent of C8 aromatic hydrocarbon | 1458 |
The device disclosed by the invention can be suitable for operation under two working conditions, and can well realize the separation of materials under the two working conditions. The device and the method can meet the requirement of product scheme change from the overall planning and can save energy to the maximum extent.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the illustrated embodiments.
Claims (9)
1. The device for the multi-working-condition operation of the nine decarbonization towers of the pyrolysis gasoline hydrogenation device is characterized by comprising the nine decarbonization towers, wherein a first feeding hole and a second feeding hole are formed in the middle of each of the nine decarbonization towers, and the first feeding hole is positioned above the second feeding hole;
the top of the nine decarburization towers is provided with a top extraction pipeline connected with a hydrogenation reaction system, and along the material flow direction, the top extraction pipeline is sequentially provided with a top condenser, a reflux tank and a top pump, the reflux tank is connected with a vacuum pumping system through a nine decarburization tower tail gas condenser, and the top extraction pipeline at the downstream of the top pump is provided with a reflux pipeline connected with the upper part of the nine decarburization towers;
a carbon eight-side line extraction pipeline and a side line extraction gas phase balance port are arranged at the middle lower part of the nine decarburization tower, a carbon eight-side line extraction control assembly, a mixer, a carbon eight-product tank, a carbon eight-product pump, a carbon eight-product cooler and a discharge valve are sequentially arranged on the carbon eight-side line extraction pipeline along the material flow direction, a return pipeline connected with the mixer is arranged on the carbon eight-side line extraction pipeline between the carbon eight-product cooler and the discharge valve, a cooling carbon eight-return control assembly is arranged on the return pipeline, and the top of the carbon eight-product tank is connected with the side line extraction gas phase balance port through a gas phase balance line;
a tower kettle extraction pipeline is arranged at the bottom of the nine decarburization tower, a tower kettle pump and a nine carbon product cooler are sequentially arranged on the tower kettle extraction pipeline along the material flow direction, and a reboiler is arranged at the bottom of the nine decarburization tower;
the tower internals of the nine decarburization towers comprise upper packing and tower plates arranged below the packing; the first feed inlet is arranged between the filler and the tower plate, and the second feed inlet is arranged at the upper part of the tower plate.
2. The device for the decarbonization nine-tower multi-operating of the pyrolysis gasoline hydrogenation unit of claim 1, wherein the carbon eight-side draw flow control assembly comprises a first thermometer, a first flow meter and a first regulating valve, the first flow meter and the first regulating valve are arranged on the carbon eight-side draw line, the first thermometer is arranged at the upper part of the tower plate, and the first regulating valve is controlled in series through the first thermometer and the first flow meter.
3. The device for the nine-tower multi-operating decarburization working condition of the pyrolysis gasoline hydrogenation unit as claimed in claim 2, wherein the height of the packing is 4-6m, and the number of the trays is 33-55; counting from top to bottom, wherein the second feed inlet is arranged at the 10 +/-3 th tower plate; the carbon eight-side-draw pipeline and the side-draw gas phase balance port are arranged at the 12 +/-3 tower plates; the first thermometer is arranged at the 2 nd to 6 th tower plates.
4. The decarbonization nine-column multi-operation apparatus for the pyrolysis gasoline hydrogenation apparatus according to claim 1, wherein the cooling carbon eight-return amount control module comprises a second thermometer, a second flow meter and a second regulating valve, the second flow meter and the second regulating valve are provided on the return line, the second thermometer is provided at the outlet of the carbon eight-product tank, and the second regulating valve is controlled in series by the second thermometer and the second flow meter.
5. The pyrolysis gasoline hydrogenation apparatus decarbonization nine-tower multi-operating-condition operation apparatus according to claim 1, wherein the tail gas condenser of the decarbonization nine-tower is cooled by using propylene refrigerant.
6. The device for decarbonizing and nine-tower multi-operating of the pyrolysis gasoline hydrogenation device of claim 1, wherein the reboiler has two, one of which is in operation and the other one is in standby.
7. The method for the decarbonization nine-tower multi-working-condition operation of the pyrolysis gasoline hydrogenation device by the device in any one of claims 1 to 6 is characterized by comprising the following steps:
the working condition I is as follows: the raw material from the five decarburization tower system enters a nine decarburization tower through a first feeding hole, and C6-C7 fractions are extracted from an extraction pipeline at the top of the tower; c8 fraction is extracted from a carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower kettle extraction pipeline;
working conditions are as follows: the raw material from the five decarbonization tower system enters a nine decarbonization tower through a second feeding hole, and C6-C8 fractions are extracted from an overhead extraction pipeline; closing the carbon eight-side line extraction pipeline; c9+ fraction is extracted from a tower bottom extraction pipeline.
8. The method for the multi-operating condition of the nine towers for the decarburization of the pyrolysis gasoline hydrogenation unit as claimed in claim 7, wherein under the operating condition, the operating flexibility of the nine towers for the decarburization is 60-110%, the operating temperature is 53-140 ℃, the operating pressure is-0.073-0.049 MPaG, the operating pressure at the top of the tower is 20-40KPaA, and the outlet temperature of the eight carbon product tank is not more than 75 ℃.
9. The multi-operating-condition operation method for the nine decarbonizing towers of the pyrolysis gasoline hydrogenation device according to claim 7, wherein under the second working condition, the operating flexibility of the nine decarbonizing towers is 60-100%, the operating temperature is 67-140 ℃, the operating pressure is-0.073-0.049 MPaG, and the operating pressure at the tops of the towers is 20-40KPaA.
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