CN111517908A - Process method and system for co-production of propane dehydrogenation device and ethylene device - Google Patents
Process method and system for co-production of propane dehydrogenation device and ethylene device Download PDFInfo
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- CN111517908A CN111517908A CN202010432185.9A CN202010432185A CN111517908A CN 111517908 A CN111517908 A CN 111517908A CN 202010432185 A CN202010432185 A CN 202010432185A CN 111517908 A CN111517908 A CN 111517908A
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- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
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- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/04—Thermal processes
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Abstract
The invention relates to a process method and a system for co-production of a propane dehydrogenation device and an ethylene device. The investment of equipment is reduced, the floor area of the equipment is reduced, and the method has higher implementation value and economic benefit.
Description
Technical Field
The invention belongs to the technical field of propane dehydrogenation and ethylene, and particularly relates to a process method and a system for co-production of an ethylene device of a propane dehydrogenation device.
Background
Ethylene and propylene are important petrochemical monomers and can be used for producing various polymers and intermediates. As the market demand for these products increases, so does the demand for ethylene and propylene. Ethylene plants and propane dehydrogenation plants are the main production plants for producing ethylene and propylene at present.
With the continuous expansion of the productivity of the newly designed device, the investment of the ethylene and propane dehydrogenation device is increased, and the occupied area is increased.
In view of the above problems, how to realize co-production of an ethylene plant and a propane dehydrogenation plant by changing a technical scheme is a problem to be solved urgently.
Disclosure of Invention
The invention aims to provide a process method and a system for co-production of a propane dehydrogenation device and an ethylene device, and aims to solve the problems of high investment and large occupied area of the conventional ethylene device and the conventional propane dehydrogenation device.
The invention is realized by the following technical scheme:
a process method for co-production of a propane dehydrogenation unit and an ethylene unit comprises the following steps:
s1, conveying the PDH product rich gas from the reaction unit to the lower side of the oil-gas water washing tower, and discharging the washed PDH product rich gas from the top of the oil-gas water washing tower;
s2, feeding the PDH product rich gas discharged from the top of the oil-gas water washing tower into a rich gas compressor, pressurizing the PDH product rich gas, and then sending the pressurized PDH product rich gas to an outlet cooler of the rich gas compressor for cooling;
s3, conveying the cooled PDH product rich gas to the upper side part of the steam-water separation tank to separate oil-containing sewage, and discharging the PDH product rich gas from the top of the steam-water separation tank;
s4, conveying the PDH product rich gas discharged from the top of the steam-water separation tank to an inlet of a rich gas dryer, removing residual moisture through the rich gas dryer, then, feeding the product rich gas into a cold box from an outlet of the rich gas dryer, and further cooling the product rich gas;
and S5, conveying the further cooled rich gas of the PDH product to the upper side part of the gas-liquid separation tank, wherein the light hydrocarbon gas is conveyed to the inlet of a fifth section compressor of cracking gas of the ethylene device from the top of the gas-liquid separation tank, and the light hydrocarbon condensate at the bottom of the gas-liquid separation tank is conveyed to the middle measuring part of the high-pressure depropanizer of the ethylene device through a condensate conveying pump.
Preferably, the method further comprises the following steps: and (3) eliminating a rectifying tower system of a propane dehydrogenation device, and conveying the PDH product rich gas of propane dehydrogenation and ethylene device cracking gas to the rectifying tower system of the ethylene device together for separation.
Preferably, the theoretical plate number of the oil-gas water washing tower in the step S1 is 4, the temperature extracted from the top of the tower is 42 ℃, the operation pressure is normal pressure, and the temperature extracted from the bottom of the tower is 55 ℃.
Preferably, the outlet pressure of the rich gas compressor is 1.75MPaG, and the outlet temperature of the hot end of the outlet cooler of the rich gas compressor is 40 ℃.
Preferably, the operating pressure of the steam-water separation tank is 1.7MPaG, and the operating temperature is 40 ℃.
Preferably, the rich gas dryer is operated at a pressure of 1.69MPaG and at a temperature of 40 ℃.
Preferably, the temperature of the rich gas inlet end of the PDH product of the cold box is 40 ℃, and the temperature of the outlet end of the cold box is-10 ℃; the operating pressure of the gas-liquid separation tank was 1.6MPaG and the operating temperature was-10 ℃.
Preferably, the PDH product rich gas comprises the following components in percentage by weight: 1.57 wt% of hydrogen, 0.86 wt% of methane, 0.49 wt% of ethylene, 0.84 wt% of ethane, 0.01 wt% of propyne, 32.11 wt% of propylene, 62.65 wt% of propane and 0.95 wt% of heavy component impurities.
A system for use in any one of the above processes for co-production of a propane dehydrogenation unit with an ethylene unit, comprising: the system comprises an oil-gas washing tower, a rich gas compressor outlet cooler, a steam-water separator, a rich gas dryer, a cold box, a gas-liquid separation tank and a condensate delivery pump;
the gas outlet of the reaction unit of the propane dehydrogenation device is connected with the lower side part of the oil-gas washing tower through a pipeline, the top part of the oil-gas washing tower is connected with the inlet of a rich gas compressor through a pipeline, the outlet of the rich gas compressor is connected with the inlet of an outlet cooler of the rich gas compressor through a pipeline, the outlet of the outlet cooler of the rich gas compressor is connected with the upper side part of a steam-water separation tank through a pipeline, the gas phase outlet at the top part of the steam-water separation tank is connected with the gas inlet of a rich gas dryer through a pipeline, the gas outlet of the rich gas dryer is connected with the rich gas inlet end of a cold box through a pipeline, the rich gas outlet end of the cold box is connected with the upper side part inlet of the gas-liquid separation tank through a pipeline, the gas phase outlet at the top part of the gas-liquid separation tank is connected with the inlet of a fifth section compressor, the outlet of the condensate delivery pump is connected with the inlet in the middle of the high-pressure depropanizing tower side of the ethylene device through a pipeline, and the outlet at the top of the high-pressure depropanizing tower of the ethylene device is connected with the inlet of a fifth section compressor of cracked gas of the ethylene device through a pipeline.
The invention has the beneficial effects that:
according to the process method for co-production of the propane dehydrogenation device and the ethylene device, a rectifying tower system of the propane dehydrogenation device is omitted, the rectifying tower system of the ethylene device is used together, the equipment investment is reduced, the occupied area of the equipment is reduced, and the process method has high implementation value and economic benefit.
Drawings
FIG. 1 is a process flow diagram for co-production of a propane dehydrogenation plant and an ethylene plant.
Description of the reference numerals
1-oil gas water washing tower; 2-a rich gas compressor; 3-a rich gas compressor outlet cooler; 4-a steam-water separation tank; 5-rich gas dryer; 6-a cold box; 7-a gas-liquid separation tank; 8-a condensate delivery pump; 9-a fifth stage compressor of cracked gas of the ethylene device; a high pressure depropanizer of a 10-ethylene plant.
Detailed Description
The technical solutions of the present invention are described in detail below by examples, and the following examples are only exemplary and can be used only for explaining and explaining the technical solutions of the present invention, but not construed as limiting the technical solutions of the present invention.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "top", "bottom", and the like, indicate orientations or positional relationships based on those shown in the drawings, are only used for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the invention, the meaning of "a plurality" is two or more unless otherwise specified.
In the description of the invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "connected" and "connected" are to be construed broadly, e.g. as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the creation of the present invention can be understood by those of ordinary skill in the art through specific situations.
The technical solution of the present invention will be described in detail with reference to the accompanying drawings and embodiments.
As shown in fig. 1, which is a process flow diagram for co-production of a propane dehydrogenation device and an ethylene device, a rich gas outlet of a waste heat recovery device of a reaction unit of the propane dehydrogenation device is connected with the lower side part of an oil-gas water washing tower 1 through a pipeline, the top part of the oil-gas water washing tower is connected with an inlet of a rich gas compressor 2 through a pipeline, an outlet of the rich gas compressor is connected with an inlet of an outlet cooler 3 of the rich gas compressor through a pipeline, an outlet of the outlet cooler of the rich gas compressor is connected with the upper side part of a steam-water separation tank 4 through a pipeline, a gas phase outlet at the top part of the steam-water separation tank is connected with a gas inlet of a rich gas drier 5 through a pipeline, a gas outlet of the rich gas drier is connected with a rich gas inlet end of a cold box 6 through a pipeline, a rich gas outlet end of the cold box is connected with an upper side inlet of a gas-liquid separation tank 7 through a pipeline, the liquid phase outlet at the bottom of the gas-liquid separation tank is connected with the inlet of a condensate delivery pump 8 through a pipeline, the outlet of the condensate delivery pump is connected with the inlet at the middle part of the side of a high-pressure depropanizing tower 10 of the ethylene device through a pipeline, and the outlet at the top of the high-pressure depropanizing tower of the ethylene device is connected with the inlet of a fifth-stage compressor of cracked gas of the ethylene device through a pipeline.
The production process of the process system for co-producing the propane dehydrogenation device and the ethylene device comprises the following steps:
s1, conveying a PDH product rich gas from a reaction unit of the propane dehydrogenation device to the lower side part of the oil-gas water washing tower, and discharging the washed PDH product rich gas from the top of the oil-gas water washing tower; in the application, the theoretical plate number of the oil-gas water washing tower is 4 layers; in this example, the composition of the PDH product rich gas by weight percentage is: 1.57 wt% of hydrogen, 0.86 wt% of methane, 0.49 wt% of ethylene, 0.84 wt% of ethane, 0.01 wt% of propyne, 32.11 wt% of propylene, 62.65 wt% of propane and 0.95 wt% of heavy component impurities.
In other embodiments of the present application, the composition of the propane feedstock and the composition or amount of each composition in the rich gas of the PDH product produced will vary and are within the scope of the present application.
In the technology of the application, the oil gas washing tower is operated under normal pressure, the temperature at the top of the tower is 42 ℃, the temperature at the bottom of the tower is 55 ℃, the temperature is the optimal temperature for the rich gas treatment of the PDH product, and in the actual production, the temperature fluctuates, which does not affect the realization of the process, but has certain influence on the yield of the corresponding product and the like.
S2, feeding a PDH product rich gas discharged from the top of the oil-gas water washing tower into a rich gas compressor, pressurizing the PDH product rich gas to 1.75MPaG, and then sending the gas to a rich gas compressor outlet cooler for cooling to 40 ℃; and discharging oily sewage from the bottom of the oil gas washing tower, and feeding the oily sewage into a recovery device to recover substances which can be utilized.
And S3, conveying the cooled PDH product rich gas to the upper side part of a steam-water separation tank, wherein the operating pressure in the steam-water separation tank is 1.7MPaG, the operating temperature is 40 ℃, the oil-containing sewage is separated from the PDH product rich gas, and the PDH product rich gas is discharged from the top of the steam-water separation tank.
And S4, conveying the PDH product rich gas discharged from the top of the steam-water separation tank to the gas inlet of a rich gas dryer, wherein the operating pressure of the rich gas dryer is 1.69MPaG, the operating temperature is 40 ℃, removing residual moisture through the rich gas dryer, then feeding the PDH product rich gas into a cold box from the gas outlet of the rich gas dryer, the inlet temperature of the PDH product rich gas of the cold box is 40 ℃, the outlet temperature of the PDH product rich gas of the cold box is-10 ℃, and further cooling.
And S5, further cooling to-10 ℃ to convey the rich gas of the PDH product to the upper side part of a gas-liquid separation tank, wherein the operating pressure of the gas-liquid separation tank is 1.6MPaG, the operating temperature is-10 ℃, the light hydrocarbon gas is conveyed from the top of the gas-liquid separation tank to the inlet of a fifth section of compressor of cracked gas of the ethylene device, and the light hydrocarbon condensate at the bottom of the gas-liquid separation tank is conveyed to the middle side part of a high-pressure depropanizer of the ethylene device through a condensate conveying pump.
The key technology of the process is to cancel a rectifying tower system of a propane dehydrogenation device and convey PDH product rich gas of propane dehydrogenation and cracking gas of an ethylene device to the rectifying tower system of the ethylene device for separation.
While the process and system for co-production of a propane dehydrogenation unit and an ethylene unit have been described by way of example, it will be apparent to those skilled in the art that the techniques of this application can be practiced by modifying or appropriately modifying or combining the products and methods of manufacture described herein without departing from the spirit, scope and spirit of the invention. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and content of this application.
Claims (9)
1. A process method for co-production of a propane dehydrogenation device and an ethylene device is characterized by comprising the following steps:
s1, conveying the PDH product rich gas from the reaction unit to the lower side of the oil-gas water washing tower, and discharging the washed PDH product rich gas from the top of the oil-gas water washing tower;
s2, feeding the PDH product rich gas discharged from the top of the oil-gas water washing tower into a rich gas compressor, pressurizing the PDH product rich gas, and then sending the pressurized PDH product rich gas to an outlet cooler of the rich gas compressor for cooling;
s3, conveying the cooled PDH product rich gas to the upper side part of the steam-water separation tank to separate oil-containing sewage, and discharging the PDH product rich gas from the top of the steam-water separation tank;
s4, conveying the PDH product rich gas discharged from the top of the steam-water separation tank to the top of a rich gas dryer, removing residual moisture through the rich gas dryer, and then entering a cold box from the bottom of the rich gas dryer for further cooling;
and S5, conveying the further cooled rich gas of the PDH product to the upper side part of the gas-liquid separation tank, wherein the light hydrocarbon gas is conveyed to the inlet of a fifth section compressor of cracking gas of the ethylene device from the top of the gas-liquid separation tank, and the light hydrocarbon condensate at the bottom of the gas-liquid separation tank is conveyed to the middle side part of the high-pressure depropanizing tower of the ethylene device through a condensate conveying pump.
2. The process for propane dehydrogenation unit and ethylene unit co-production according to claim 1, further comprising: the process method cancels a rectifying tower system of a propane dehydrogenation device, and conveys PDH product rich gas of propane dehydrogenation and cracking gas of an ethylene device to the rectifying tower system of the ethylene device for separation.
3. The process for co-production of a propane dehydrogenation unit and an ethylene unit according to claim 1, wherein the theoretical plate number of the oil gas water washing tower in the step S1 is 4, the temperature extracted from the top of the tower is 42 ℃, the operating pressure is normal pressure, and the temperature extracted from the bottom of the tower is 55 ℃.
4. The process for the co-production of a propane dehydrogenation unit and an ethylene unit of claim 1, wherein the rich gas compressor outlet pressure is 1.75MPaG and the rich gas compressor outlet cooler hot end outlet temperature is 40 ℃.
5. The process for the co-production of a propane dehydrogenation unit and an ethylene unit of claim 1, wherein the steam-water separation tank is operated at a pressure of 1.7MPaG and at a temperature of 40 ℃.
6. The process for the co-production of a propane dehydrogenation unit and an ethylene unit of claim 1, wherein the rich gas dryer is operated at a pressure of 1.69MPaG and at a temperature of 40 ℃.
7. The process for the co-production of a propane dehydrogenation unit and an ethylene unit according to claim 1, wherein the PDH product rich gas of the cold box has an inlet temperature of 40 ℃ and an outlet temperature of-10 ℃; the operating pressure of the gas-liquid separation tank was 1.6MPaG and the operating temperature was-10 ℃.
8. The process for propane dehydrogenation unit and ethylene unit co-production according to claim 1, wherein the composition of the PDH product rich gas in weight percent is: 1.57 wt% of hydrogen, 0.86 wt% of methane, 0.49 wt% of ethylene, 0.84 wt% of ethane, 0.01 wt% of propyne, 32.11 wt% of propylene, 62.65 wt% of propane and 0.95 wt% of heavy component impurities.
9. A system for use in a process for co-production of a propane dehydrogenation unit with an ethylene unit according to any of the preceding claims 1 to 8, comprising: the system comprises an oil-gas washing tower, a rich gas compressor outlet cooler, a steam-water separator, a rich gas dryer, a cold box, a gas-liquid separation tank and a condensate delivery pump;
a rich gas outlet of a waste heat recovery device of a reaction unit of a propane dehydrogenation device is connected with the lower side part of an oil gas washing tower through a pipeline, the top part of the oil gas washing tower is connected with an inlet of a rich gas compressor through a pipeline, an outlet of the rich gas compressor is connected with an inlet of an outlet cooler of the rich gas compressor through a pipeline, an outlet of the outlet cooler of the rich gas compressor is connected with the upper side part of a steam-water separation tank through a pipeline, a gas phase outlet at the top part of the steam-water separation tank is connected with a gas inlet of a rich gas drier through a pipeline, a gas outlet of the rich gas drier is connected with a rich gas inlet end of a cold box through a pipeline, a rich gas outlet end of the cold box is connected with an upper side part inlet of the gas-liquid separation tank through a pipeline, a gas phase outlet at the top part of the gas-liquid separation tank is connected with an inlet of a fifth section of, the outlet of the condensate delivery pump is connected with the inlet in the middle of the high-pressure depropanizing tower side of the ethylene device through a pipeline, and the outlet at the top of the high-pressure depropanizing tower of the ethylene device is connected with the inlet of a fifth section compressor of cracked gas of the ethylene device through a pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010432185.9A CN111517908A (en) | 2020-05-20 | 2020-05-20 | Process method and system for co-production of propane dehydrogenation device and ethylene device |
| PCT/CN2020/092433 WO2021232453A1 (en) | 2020-05-20 | 2020-05-26 | Process method and system for co-production of propane dehydrogenation device and ethylene device |
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| CN202010432185.9A CN111517908A (en) | 2020-05-20 | 2020-05-20 | Process method and system for co-production of propane dehydrogenation device and ethylene device |
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| CN107673947A (en) * | 2017-10-11 | 2018-02-09 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique |
| CN108456128A (en) * | 2018-06-05 | 2018-08-28 | 北京恒泰洁能科技有限公司 | A kind of separating technology and system of dehydrogenating propane product gas |
| CN109761734A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and ethane cracking front-end deethanization are coupled with PDH |
| CN109734549A (en) * | 2019-01-21 | 2019-05-10 | 中石化上海工程有限公司 | Naphtha and Deposition During Propane Pyrolysis sequentially separate the method coupled with PDH |
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- 2020-05-20 CN CN202010432185.9A patent/CN111517908A/en active Pending
- 2020-05-26 WO PCT/CN2020/092433 patent/WO2021232453A1/en active Application Filing
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| CN110944967A (en) * | 2017-07-12 | 2020-03-31 | 林德股份公司 | Process and plant for the production of propylene combining a propane dehydrogenation and a steam cracking process, in both of which there is a preliminary separation step for partial removal of hydrogen and methane |
| CN109809957A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique |
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