CN111377791A - Method for reducing energy consumption of ethylbenzene device by using recycle benzene - Google Patents
Method for reducing energy consumption of ethylbenzene device by using recycle benzene Download PDFInfo
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- CN111377791A CN111377791A CN202010196043.7A CN202010196043A CN111377791A CN 111377791 A CN111377791 A CN 111377791A CN 202010196043 A CN202010196043 A CN 202010196043A CN 111377791 A CN111377791 A CN 111377791A
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- ethylbenzene
- benzene
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
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Abstract
The invention relates to a method for reducing energy consumption of an ethylbenzene device by using recycle benzene, which comprises the following steps: a. a heat exchanger is added in front of an extraction cooler of an ethylbenzene processing device, ethylbenzene is removed on a shell pass, and fresh benzene is removed on a tube pass; b. after heat exchange is carried out between the hot ethylbenzene and the fresh benzene at normal temperature through a heat exchanger, the hot ethylbenzene led out by an ethylbenzene processing device is subjected to cooling treatment; c. fresh benzene in a tube pass is subjected to heat exchange through a heat exchanger and then enters a heating furnace of an ethylbenzene processing device for further processing ethylbenzene through heating and pressurizing treatment, and the process performs heat exchange through the fresh benzene and extracted high-temperature ethylbenzene to achieve the purposes of improving the temperature of the fresh benzene and reducing the temperature of extracted ethylbenzene, so that the pressure and the outlet temperature of a buffer tank are improved, the gas-phase method circulating benzene achieves the autogenous pressure condition, the load of the heating furnace is reduced, and the energy consumption of the ethylbenzene device is finally reduced.
Description
Technical Field
The invention relates to the field of petrochemical production, in particular to a method for reducing energy consumption of an ethylbenzene device by using recycle benzene.
Background
At present, the production of ethylbenzene mainly adopts dry gas method and liquid phase method, the liquid phase method is a process for synthesizing ethylbenzene by alkylation reaction of pure ethylene and benzene under the action of liquid phase molecular sieve catalyst, and said process is characterized by that the reaction is implemented in liquid phase, and the interior of reactor has no temp. runaway, and adopts Y-type (or β type) molecular sieve with pore size, and its reaction production is smooth, and has no need of higher reaction temp.
① causes the increase of side reaction, increases the difficulty of removing by-products of a rectification system, mainly increases the difficulty of removing by-products by the rectification system, mainly leads to higher content of dimethylbenzene in products because the dimethylbenzene is difficult to remove by a rectification mode, finally enters a finished product ② after various gas components which do not need to react are heated, enters a reaction and fractionation system, increases the energy consumption, material consumption and single consumption loss of a catalyst.
The dry gas method and the liquid phase method are combined to prepare ethylbenzene, a circulating benzene buffer tank is shared, the amount of fresh benzene required to be supplemented after the liquid phase method is increased is large, a large amount of normal-temperature fresh benzene and gas-phase benzene at 188 ℃ on the benzene tower side line are mixed and then enter the circulating benzene buffer tank, and the pressure of the circulating benzene buffer tank is basically brought by the benzene tower side line, so that the pressure of the circulating benzene buffer tank is low and basically about 0.5MPa after the large amount of normal-temperature fresh benzene enters, and meanwhile, the outlet temperature is low and is about 135 ℃. And then the recycle benzene of the dry gas method can not reach the autogenous pressure condition (the pressure of the recycle benzene buffer tank is more than 0.75 MPa), the operation can be maintained only by P-26202, the inlet temperature of the gas phase reactor is controlled by a recycle benzene heating furnace, the load of the heating furnace is directly increased after the outlet temperature of the recycle benzene buffer tank is reduced, the energy consumption of the device is greatly increased, in addition, after the extraction amount of the ethylbenzene is increased, the temperature of the ethylbenzene tank extracted to the tank area is higher (about 70 ℃) due to the limitation of a cooler, and the temperature range limit received by the tank area is already approached quickly.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provides a method for reducing the energy consumption of an ethylbenzene device by using recycle benzene.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a method for reducing energy consumption of an ethylbenzene plant by using recycled benzene comprises the following steps:
a. a heat exchanger is added in front of an extraction cooler of an ethylbenzene processing device, ethylbenzene is removed on a shell pass, and fresh benzene is removed on a tube pass;
b. after heat exchange is carried out between the hot ethylbenzene and the fresh benzene at normal temperature through a heat exchanger, the hot ethylbenzene led out by an ethylbenzene processing device is subjected to cooling treatment;
c. after heat exchange of fresh benzene in the tube pass is carried out by a heat exchanger, the fresh benzene enters a heating furnace of an ethylbenzene processing device for further processing ethylbenzene by heating and pressurizing treatment.
Further, after heat exchange is carried out between hot ethylbenzene led out by the ethylbenzene processing device and normal-temperature fresh benzene through a heat exchanger, the temperature of the hot ethylbenzene is reduced to 40-60 ℃ from about 70 ℃, and after the hot ethylbenzene is cooled through circulating water in an E26205N circulating tank, the extraction temperature of the ethylbenzene is finally reduced to be within 40 ℃ and is sent to a tank area.
Further, after heat exchange is carried out between hot ethylbenzene led out by the ethylbenzene processing device and normal-temperature fresh benzene through a heat exchanger, the temperature of the hot ethylbenzene is reduced to 50 ℃ from about 70 ℃, and after the hot ethylbenzene is cooled through circulating water in an E26205N circulating tank, the extraction temperature of the ethylbenzene is finally reduced to be within 40 ℃ and is sent to a tank area.
Further, the fresh benzene in the tube pass is subjected to heat exchange by a heat exchanger and then rises from the normal temperature to 40-50 ℃, then is mixed with lateral benzene and enters a V-26101 circulating benzene buffer tank, the pressure of the V-26101 circulating benzene buffer tank is increased to be more than 0.85MPa, and the temperature of outlet circulating benzene rises from 135 ℃ to 150 ℃ and then enters a heating furnace through a circulating benzene evaporator.
Further, the fresh benzene in the tube pass is subjected to heat exchange by a heat exchanger and then rises to 45 ℃ from the normal temperature, then is mixed with lateral line benzene at 193 ℃ and enters a V-26101 circulating benzene buffer tank, the pressure of the V-26101 circulating benzene buffer tank is increased to be more than 0.85MPa, and the temperature of outlet circulating benzene rises to 150 ℃ from 135 ℃ and then enters a heating furnace through a circulating benzene evaporator.
Further, the temperature of the outlet circulating benzene rises from 135 ℃ to 150 ℃, then the outlet circulating benzene enters the heating furnace through the circulating benzene evaporator, and the temperature of the outlet of the heating furnace is controlled by 320-330 ℃ through adjusting the fuel gas amount of the heating furnace.
The invention has the beneficial effects that: according to the process, heat exchange is carried out between fresh benzene and extracted high-temperature ethylbenzene to achieve the purposes of increasing the temperature of the fresh benzene and reducing the temperature of the extracted ethylbenzene, so that the pressure and the outlet temperature of a buffer tank are increased, the gas-phase method circulating benzene is enabled to reach the self-pressure condition, the load of a heating furnace is reduced, and the energy consumption of an ethylbenzene device is finally reduced.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention.
Detailed Description
As shown in fig. 1, a method for reducing the energy consumption of an ethylbenzene plant using recycle benzene comprises the following steps:
a. a heat exchanger is added in front of an extraction cooler of an ethylbenzene processing device, ethylbenzene is removed on a shell pass, and fresh benzene is removed on a tube pass;
b. after heat exchange is carried out between the hot ethylbenzene and the fresh benzene at normal temperature through a heat exchanger, the hot ethylbenzene led out by an ethylbenzene processing device is subjected to cooling treatment;
c. after heat exchange of fresh benzene in the tube pass is carried out by a heat exchanger, the fresh benzene enters a heating furnace of an ethylbenzene processing device for further processing ethylbenzene by heating and pressurizing treatment.
After heat exchange is carried out between hot ethylbenzene led out by an ethylbenzene processing device and normal-temperature fresh benzene through a heat exchanger, the temperature of the hot ethylbenzene is reduced to 40-60 ℃ from about 70 ℃, and after the hot ethylbenzene is cooled through circulating water in an E26205N circulating tank, the extraction temperature of the ethylbenzene is finally reduced to be within 40 ℃ and is sent to a tank area.
The method specifically comprises the following steps: after heat exchange is carried out between hot ethylbenzene led out by an ethylbenzene processing device and normal-temperature fresh benzene through a heat exchanger, the temperature of the hot ethylbenzene is reduced to 50 ℃ from about 70 ℃, and after the hot ethylbenzene is cooled through circulating water in an E26205N circulating tank, the extraction temperature of the ethylbenzene is finally reduced to be within 40 ℃ and is sent to a tank area.
In addition, the fresh benzene in the tube pass is subjected to heat exchange by a heat exchanger and then rises to 40-50 ℃ from the normal temperature, then is mixed with lateral benzene and enters a V-26101 circulating benzene buffer tank, the pressure of the V-26101 circulating benzene buffer tank is increased to be more than 0.85MPa, and the temperature of outlet circulating benzene rises to 150 ℃ from 135 ℃ and then enters a heating furnace through a circulating benzene evaporator.
The method specifically comprises the following steps: fresh benzene in a tube pass is subjected to heat exchange by a heat exchanger and then rises to 45 ℃ from the normal temperature, then is mixed with lateral benzene at 193 ℃ and enters a V-26101 circulating benzene buffer tank, the pressure of the V-26101 circulating benzene buffer tank is increased to be more than 0.85MPa, the temperature of outlet circulating benzene rises to be 150 ℃ from 135 ℃, then the mixture enters a heating furnace through a circulating benzene evaporator, and the fuel gas of the heating furnace is adjusted to control the outlet temperature of the furnace to be 320-.
The specific indexes of the invention are that the pressure of the ① recycle benzene buffer tank is controlled to be above 0.85MPa, the outlet temperature of the ② recycle benzene buffer tank is controlled to be 145-150 ℃, and the extraction temperature of ③ ethylbenzene is controlled to be below 45 ℃.
According to the process, heat exchange is carried out between fresh benzene and extracted high-temperature ethylbenzene to achieve the purposes of increasing the temperature of the fresh benzene and reducing the temperature of the extracted ethylbenzene, so that the pressure and the outlet temperature of a buffer tank are increased, the gas-phase method circulating benzene is enabled to reach the self-pressure condition, the load of a heating furnace is reduced, and the energy consumption of an ethylbenzene device is finally reduced.
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are merely illustrative of the principles of the invention, but that various changes and modifications may be made without departing from the spirit and scope of the invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (6)
1. A method for reducing energy consumption of an ethylbenzene plant by using recycle benzene is characterized by comprising the following steps:
a. a heat exchanger is added in front of an extraction cooler of an ethylbenzene processing device, ethylbenzene is removed on a shell pass, and fresh benzene is removed on a tube pass;
b. after heat exchange is carried out between the hot ethylbenzene and the fresh benzene at normal temperature through a heat exchanger, the hot ethylbenzene led out by an ethylbenzene processing device is subjected to cooling treatment;
c. after heat exchange of fresh benzene in the tube pass is carried out by a heat exchanger, the fresh benzene enters a heating furnace of an ethylbenzene processing device for further processing ethylbenzene by heating and pressurizing treatment.
2. The method for reducing the energy consumption of the ethylbenzene plant by using the recycle benzene as claimed in claim 1, wherein the hot ethylbenzene discharged from the ethylbenzene processing plant is subjected to heat exchange with fresh benzene at normal temperature through a heat exchanger, the temperature of the hot ethylbenzene is reduced from about 70 ℃ to 40-60 ℃, and after the hot ethylbenzene is cooled by the recycle water in the E26205N recycle tank, the extraction temperature of the ethylbenzene is finally reduced to within 40 ℃ and sent to the tank area.
3. The method for reducing the energy consumption of the ethylbenzene plant by using the recycle benzene as claimed in claim 2, wherein the hot ethylbenzene discharged from the ethylbenzene processing plant is subjected to heat exchange with fresh benzene at normal temperature through a heat exchanger, the temperature of the hot ethylbenzene is reduced from about 70 ℃ to 50 ℃, and after the hot ethylbenzene is cooled by the recycle water in the E26205N recycle tank, the extraction temperature of the ethylbenzene is finally reduced to within 40 ℃ and is sent to the tank area.
4. The method for reducing the energy consumption of the ethylbenzene plant by using the recycle benzene as claimed in claim 2, wherein the fresh benzene in the tube pass is subjected to heat exchange by a heat exchanger, then is increased from the normal temperature to 40-50 ℃, is mixed with the side-line benzene, and then enters the V-26101 recycle benzene buffer tank, the pressure of the V-26101 recycle benzene buffer tank is increased to more than 0.85MPa, and the temperature of the outlet recycle benzene is increased from 135 ℃ to 150 ℃ and then enters the heating furnace through the recycle benzene evaporator.
5. The method for reducing the energy consumption of the ethylbenzene plant by using the recycle benzene as claimed in claim 4, wherein the fresh benzene in the tube pass is subjected to heat exchange by a heat exchanger, then is increased from the normal temperature to 45 ℃, is mixed with the side-line benzene at 193 ℃ and then enters the V-26101 recycle benzene buffer tank, the pressure of the V-26101 recycle benzene buffer tank is increased to be above 0.85MPa, and the temperature of the outlet recycle benzene is increased from 135 ℃ to 150 ℃ and then enters the heating furnace through the recycle benzene evaporator.
6. The method as claimed in claim 5, wherein the temperature of the outlet recycle benzene rises from 135 ℃ to 150 ℃ and then enters the heating furnace through the recycle benzene evaporator, and the fuel gas of the heating furnace is adjusted to control the outlet temperature of the furnace to 320 ℃ and 330 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010196043.7A CN111377791A (en) | 2020-03-19 | 2020-03-19 | Method for reducing energy consumption of ethylbenzene device by using recycle benzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010196043.7A CN111377791A (en) | 2020-03-19 | 2020-03-19 | Method for reducing energy consumption of ethylbenzene device by using recycle benzene |
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| CN111377791A true CN111377791A (en) | 2020-07-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010196043.7A Withdrawn CN111377791A (en) | 2020-03-19 | 2020-03-19 | Method for reducing energy consumption of ethylbenzene device by using recycle benzene |
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| CN (1) | CN111377791A (en) |
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2020
- 2020-03-19 CN CN202010196043.7A patent/CN111377791A/en not_active Withdrawn
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Address after: 315803 No. 98 Qijiashan Port Road, Beilun District, Ningbo City, Zhejiang Province Applicant after: Ningbo Keyuan Jinghua Co., Ltd Address before: 315000 No. 98 Qijiashan Port Road, Beilun District, Ningbo City, Zhejiang Province Applicant before: NINGBO KEYUAN PETROCHEMICALS Co.,Ltd. |
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Application publication date: 20200707 |
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