CN114835548A - Branching separation device and separation method for liquid raw material steam cracking product and gas raw material steam cracking product - Google Patents
Branching separation device and separation method for liquid raw material steam cracking product and gas raw material steam cracking product Download PDFInfo
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- 239000002994 raw material Substances 0.000 title claims abstract description 252
- 239000007788 liquid Substances 0.000 title claims abstract description 174
- 238000000926 separation method Methods 0.000 title claims abstract description 106
- 238000004230 steam cracking Methods 0.000 title claims abstract description 41
- 238000005336 cracking Methods 0.000 claims abstract description 201
- 230000006835 compression Effects 0.000 claims abstract description 111
- 238000007906 compression Methods 0.000 claims abstract description 111
- 238000010791 quenching Methods 0.000 claims abstract description 101
- 230000000171 quenching effect Effects 0.000 claims abstract description 94
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 67
- 239000005977 Ethylene Substances 0.000 claims abstract description 67
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 66
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 54
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 50
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 42
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 39
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 39
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 36
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 27
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 27
- 239000001294 propane Substances 0.000 claims abstract description 21
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000001273 butane Substances 0.000 claims abstract description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 4
- 230000009467 reduction Effects 0.000 claims description 18
- 238000007599 discharging Methods 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 7
- 238000000197 pyrolysis Methods 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000000126 substance Substances 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 122
- 238000012545 processing Methods 0.000 description 7
- 238000009826 distribution Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000003776 cleavage reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 230000007017 scission Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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Abstract
The invention belongs to the field of chemical industry, and relates to a branching line separation device and a separation method for a liquid raw material and a gas raw material steam cracking product. The device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route; the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system, a liquid raw material cracking product quenching water system, a first compression system, a front-cooling demethanizing system, an ethane removal system, a carbon dioxide hydrogenation system, a liquid route ethylene tower system, a propane removal system, a carbon three hydrogenation system, a propylene tower system and a butane removal system which are sequentially connected; the separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system and an optional second compression system, a front deethanization system and a third compression system which are connected in sequence. The invention can optimize the process configuration, reduce the investment, reduce the energy consumption and save the occupied area.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a branching separation device for a liquid raw material steam cracking product and a gas raw material steam cracking product, and a branching separation method for the liquid raw material steam cracking product and the gas raw material steam cracking product.
Background
Ethylene is an important basic chemical raw material, and the yield of ethylene, the scale and the technical level of a single set of equipment, the technical development capacity and the engineering capacity are marks of the development level of the petrochemical industry. In recent years, the ethylene industry has been becoming more and more integrated in refining and large in size.
As refineries move to chemical refineries, the feedstocks for steam cracking units are increasingly diverse, and large amounts of gaseous feedstocks must be processed while large amounts of liquid feedstocks are processed. With the increasing complexity and scale of the raw materials, the design difficulty and operation difficulty of the steam cracking device are increased.
In the prior art (as shown in figure 1), the liquid raw material cracking product and the gas raw material cracking product are separated in the same separation process. Because the components of the liquid raw material cracked product and the gas raw material cracked product have large distribution difference and different characteristics, the separation unit is very difficult to process the two cracked products simultaneously. In the cracking furnace unit, compared with a cracking liquid raw material, a cracking gas raw material is insensitive to the pressure at the outlet of the cracking furnace, so that the pressure at the outlet of the cracking furnace can be properly increased to reduce the power of a cracking gas compressor of the separation unit. In the quenching unit, the quenching oil tower processes the cracking product mixture with larger difference between light and heavy, and the design of a tray oil section and a quenching oil section is difficult. In the compression unit, when the apparatus is enlarged, the large-sized compressor unit is controlled by the manufacturing limit.
In order to meet the requirement of processing chemical refineries to provide both large quantities of liquid feedstock and large quantities of gaseous feedstock, it is highly desirable to develop a steam cracking apparatus and method for processing the gaseous feedstock and the liquid feedstock separately.
Disclosure of Invention
In order to meet the requirement of processing chemical refineries to simultaneously provide a large volume of liquid feedstock and a large volume of gaseous feedstock, the present invention provides a method for processing both gaseous and liquid feedstocks in a steam cracker for sequential processing. Different separation methods are adopted for different raw materials, a sequential process is adopted for a liquid phase raw material, and a front deethanization process is adopted for a gas phase raw material. At the appropriate location, the two flows converge.
In order to achieve the above object, the present invention provides a branching separation apparatus for a liquid raw material steam cracking product and a gas raw material steam cracking product, the apparatus comprising a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system, a liquid raw material cracking product quenching water system, a first compression system, a front-cooling demethanizing system, an ethane removal system, a carbon dioxide hydrogenation system, a liquid route ethylene tower system, a propane removal system, a carbon three hydrogenation system, a propylene tower system and a butane removal system which are sequentially connected; the light component discharge line of the first compression system is connected with the front-cooling demethanizing system, and the heavy component discharge line of the first compression system is connected with the depropanizing system; a discharging pipeline at the top of the deethanizer system is connected with the carbon dioxide hydrogenation system, and a discharging pipeline at the bottom of the deethanizer system is connected with the depropanization system; a tower top discharge pipeline of the depropanization system is sequentially connected with the carbon three-hydrogenation system and the propylene tower system, and a tower bottom discharge pipeline of the depropanization system is connected with the debutanization system;
the separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system, and an optional second compression system, a front deethanization system and a third compression system which are connected in sequence; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with a quenching oil system of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system of a gas raw material cracking product;
a discharge pipeline of the gas raw material cracking product quenching water system is connected with the first compression system; alternatively, the discharge line of the gaseous feed pyrolysis product quench water system is connected to the second compression system.
According to the present invention, the separation route of the gaseous raw material cracked product may adopt various processes, and when the separation routes are different, the corresponding materials are merged into the separation route of the liquid raw material cracked product at different positions, as shown in fig. 2.
According to the aforementioned first embodiment, the gaseous feedstock cracked product separation line includes a gaseous feedstock cracked product feed line and a gaseous feedstock cracked product quench water system, the discharge line of which is connected to the first compression system.
According to a second embodiment of the present invention, the separation route of the gaseous raw material cracking product further includes a second compression system, a front deethanization system, and a third compression system, wherein a discharge line of the second compression system is connected to the front deethanization system, a still discharge line of the deethanization column of the front deethanization system is connected to the depropanization system, a top discharge line of the deethanization column of the front deethanization system is connected to the third compression system, and a discharge line of the third compression system is connected to the front cold demethanization system. Namely, the separation route of the gas raw material cracked product comprises a gas raw material cracked product feed pipeline, a gas raw material cracked product quenching water system, a second compression system, a front deethanization system and a third compression system; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with a quenching oil system of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system of a gas raw material cracking product; the discharge pipeline of the second compression system is connected with the front deethanization system, the discharge pipeline of the deethanization tower kettle of the front deethanization system is connected with the depropanization system, the discharge pipeline of the deethanization tower top of the front deethanization system is connected with the third compression system, and the discharge pipeline of the third compression system is connected with the front cold demethanization system.
According to a third embodiment of the present invention, the separation route of the cracked product of the gaseous raw material further includes a pre-hydrogenation system and a demethanization system on the basis of the second embodiment, in this way, the discharge line of the third compression system is connected with the pre-hydrogenation system and the demethanization system in turn, and the discharge line of the demethanization system is connected with the ethylene column system of the liquid route. Namely, the separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system, a second compression system, a front deethanization system, a third compression system, a front hydrogenation system and a demethanization system; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with a quenching oil system of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system of a gas raw material cracking product; the discharge pipeline of the second compression system is connected with the front deethanization system, the deethanization tower kettle discharge pipeline of the front deethanization system is connected with the depropanization system, the deethanization tower top discharge pipeline of the front deethanization system is connected with the third compression system, the discharge pipeline of the third compression system is sequentially connected with the front hydrogenation system and the demethanization system, and the discharge pipeline of the demethanization system is connected with the liquid route ethylene tower system.
According to a fourth embodiment of the present invention, the separation route of the cracked product of the gaseous raw material further comprises a system of a gaseous route ethylene tower, and the discharge line of the demethanizer system is connected with the system of the gaseous route ethylene tower. Namely, the separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system, a second compression system, a front deethanization system, a third compression system, a front hydrogenation system, a demethanization system and a gas route ethylene tower system; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with a quenching oil system of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system of a gas raw material cracking product; the discharge pipeline of the second compression system is connected with the front deethanization system, the deethanization tower kettle discharge pipeline of the front deethanization system is connected with the depropanization system, the deethanization tower top discharge pipeline of the front deethanization system is connected with the third compression system, the discharge pipeline of the third compression system is sequentially connected with the front hydrogenation system and the demethanization system, and the discharge pipeline of the demethanization system is connected with the gas route ethylene tower system.
According to the invention, the liquid feedstock cracking product feed line is connected to the liquid cracking furnace outlet, and the gaseous feedstock cracking product feed line is connected to the gas cracking furnace outlet.
According to the invention, the liquid route ethylene column system and the gas route ethylene column system are each provided with an overhead ethylene discharge line and a still ethane discharge line.
According to the invention, the propylene column system is provided with an overhead propylene discharge line and a still propane discharge line.
The quench oil system generally includes a viscosity reducing column, preferably one of the gaseous feed cracked product feed lines is connected to the viscosity reducing column in the quench oil system of the liquid feed cracked product separation line.
The invention also provides a branching separation method of the liquid raw material steam cracking product and the gas raw material steam cracking product, which is carried out by adopting the branching separation device of the liquid raw material steam cracking product and the gas raw material steam cracking product, and comprises the following steps:
the liquid raw material cracked product from the liquid cracking furnace sequentially enters a quenching oil system, a liquid raw material cracked product quenching water system, a first compression system, a front-cooling demethanization system and a deethanization system; the carbon dioxide fraction obtained from the top of the deethanizer system sequentially enters the carbon dioxide hydrogenation system and the liquid route ethylene tower system to separate ethylene and ethane (which can be used as circulating ethane), and the carbon three fraction obtained from the deethanizer kettle of the deethanizer system and the heavy component generated by the first compression system enter the depropanizer system; the carbon three fraction separated from the top of the depropanizing tower of the depropanizing system enters the carbon three hydrogenation system for hydrogenation, then enters the propylene tower system for separating propylene and propane, and the material in the bottom of the depropanizing tower of the depropanizing system enters a debutanizing system (which can be used as circulating propane);
one part (preferably a small part) of the gas raw material cracking products from the gas cracking furnace enter a quenching oil system of a liquid raw material cracking product separation line for viscosity reduction, and the other part (preferably a large part) of the gas raw material cracking products enter a quenching water system of the gas raw material cracking products;
the gas raw material cracking product after passing through the gas raw material cracking product quenching water system is converged with the liquid raw material cracking product after passing through the liquid raw material cracking product quenching water system, and the gas raw material cracking product and the liquid raw material cracking product enter a first compression system together; or the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters a second compression system.
Corresponding to the various embodiments described above, the present invention also includes a variety of treatment methods.
Corresponding to the first embodiment, the gas raw material cracked product after passing through the gas raw material cracked product quenching water system is merged with the liquid raw material cracked product after passing through the liquid raw material cracked product quenching water system, and then the merged gas raw material cracked product and the liquid raw material cracked product enter the first compression system and then enter the front cooling demethanization system of the liquid raw material cracked product separation route.
Corresponding to the second embodiment, the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters the second compression system and then enters the front deethanization system, the carbon three and above fractions separated by the front deethanization system enter the depropanization system of the liquid raw material cracking product separation route, and the carbon two and below fractions separated by the front deethanization system enter the third compression system and then are merged into the liquid route front cold demethanization system.
Corresponding to the third embodiment, the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters the second compression system and then enters the front deethanization system, the carbon three and above fractions separated by the front deethanization system enter the depropanization system of the liquid raw material cracking product separation route, the carbon two and below fractions separated by the front deethanization system enter the third compression system, the front hydrogenation system and the demethanization system in sequence, and the carbon two fraction separated by the demethanization system is converged into the liquid route ethylene tower system.
Corresponding to the fourth embodiment, the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters the second compression system and then enters the front deethanization system, the carbon three and above fractions separated by the front deethanization system enter the depropanization system of the liquid raw material cracking product separation route, the carbon two and below fractions separated by the front deethanization system enter the third compression system, the front hydrogenation system and the demethanization system in sequence, and the carbon two fraction separated by the demethanization system enters the gas route ethylene tower system to obtain ethylene and ethane (which can be used as recycle ethane).
In the present invention, the concept of "gas raw material" and "liquid raw material" is known to those skilled in the art. The liquid raw materials include but are not limited to light hydrocarbon with five or more carbon atoms, naphtha, diesel oil and hydrogenated tail oil. The gaseous feedstocks include, but are not limited to, ethane, propane, butane, refinery dry gas, LPG.
The invention provides a method for processing a gas raw material and a liquid raw material by a steam cracking device. Different separation methods are adopted for different raw materials, a sequential flow is adopted for a liquid phase raw material, a front deethanization flow is adopted for a gas phase raw material, and the two flows are converged or separated at a proper position. Therefore, the purposes of optimizing the process configuration, reducing the investment and reducing the energy consumption are achieved. The invention can be implemented in the capacity expansion transformation of the existing ethylene plant, and can also be implemented in a newly-built ethylene plant.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
Figure 1 shows a flow diagram of a prior art separation technique.
FIG. 2 shows a flow diagram of a steam cracker of the present invention for processing a gaseous feed and a liquid feed.
Fig. 3 shows a flowchart of embodiment 1.
Fig. 4 shows a flowchart of embodiment 2.
Fig. 5 shows a flowchart of embodiment 3.
Fig. 6 shows a flowchart of embodiment 4.
Figure 7 shows a typical gaseous feed (ethane) and liquid feed (naphtha) cracking product distribution. Wherein, in the histogram corresponding to each component, the left side represents naphtha, and the right side represents ethane.
Description of the reference numerals
a. A liquid feedstock; b. a gaseous feed;
l-1, a liquid cracking furnace; l-2, a quench oil system; l-3, a liquid raw material cracking product quenching water system; l-4, a first compression system; l-5, pre-cold demethanization system; l-6, deethanization system; l-7, a carbon two hydrogenation system; l-8, an ethylene column system; l-9, a depropanization system; l-10, carbon three hydrogenation system; l-11, a propylene column system; l-12, debutanization system;
g-1, a gas cracking furnace; g-2, a quenching water system for a gas raw material cracking product; g-3, a second compression system; g-4, a front deethanization system; g-5, a third compression system; g-6, a front hydrogenation system; g-7, a demethanization system; g-8, gas route ethylene column system.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
Example 1
The branching separation device and the separation method of the liquid raw material steam cracking product and the gas raw material steam cracking product are adopted as shown in fig. 3.
The device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system L-2, a liquid raw material cracking product quenching water system L-3, a first compression system L-4, a front cooling demethanization system L-5, an ethane removal system L-6, a carbon dioxide hydrogenation system L-7, a liquid route ethylene tower system L-8, a propane removal system L-9, a carbon three hydrogenation system L-10, a propylene tower system L-11 and a debutaning system L-12 which are sequentially connected; the liquid raw material cracking product feeding pipeline is connected with an outlet L-1 of the liquid cracking furnace; a light component discharge pipeline of the first compression system L-4 is connected with the front cold demethanizing system L-5, and a heavy component discharge pipeline of the first compression system L-4 is connected with the depropanizing system L-9; a discharging pipeline at the top of the deethanizer system L-6 is connected with a carbon dioxide hydrogenation system L-7, and a discharging pipeline at the bottom of the deethanizer system L-6 is connected with a depropanization system L-9; a tower top discharge pipeline of the depropanization system L-9 is sequentially connected with the C-C hydrogenation system L-10 and the propylene tower system L-11, and a tower bottom discharge pipeline of the depropanization system L-9 is connected with the debutanizing system L-12; the liquid route ethylene tower system L-8 is provided with a tower top ethylene discharge pipeline and a tower kettle ethane discharge pipeline; the propylene tower system L-11 is provided with a tower top propylene discharge pipeline and a tower bottom propane discharge pipeline.
The separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline and a gas raw material cracking product quenching water system G-2; the gas raw material cracking product feeding pipeline is connected with an outlet of a gas cracking furnace G-1 and is divided into two branches, one branch is connected with a viscosity reduction tower of a quenching oil system L-2 of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system G-2 of a gas raw material cracking product; and the discharge pipeline of the gas raw material cracking product quenching water system G-2 is connected with the first compression system L-4.
The separation method comprises the following steps:
the liquid raw material a enters a liquid cracking furnace L-1 for steam cracking, and the obtained liquid raw material cracking product is separated by adopting the sequential flow: the liquid raw material cracked product sequentially enters a quenching oil system L-2, a quenching water system L-3 of the liquid raw material cracked product, a first compression system L-4, a front-cooling demethanization system L-5 and a deethanization system L-6; the carbon dioxide fraction obtained from the top of the deethanizer system L-6 sequentially enters the carbon dioxide hydrogenation system L-7 and the liquid route ethylene tower system L-8 to separate ethylene and recycle ethane, and the carbon three fraction obtained from the deethanizer tower kettle of the deethanizer system L-6 and the heavy component generated by the first compression system L-4 enter the depropanization system L-9; and the carbon three-fraction separated from the top of the depropanizing tower of the depropanizing system L-9 enters the carbon three-hydrogenation system L-10 for hydrogenation, then enters the propylene tower system L-11 for separating propylene and circulating propane, and the material at the bottom of the depropanizing tower of the depropanizing system L-9 enters the debutanizing system L-12.
And the gas raw material b enters a gas cracking furnace G-1 for steam cracking, and the obtained gas raw material cracking product mostly enters a gas raw material cracking product quenching water system G-2 except for removing a small amount of viscosity reduction tower viscosity reduction in a liquid raw material cracking product separation line for viscosity reduction. The gas raw material cracked product passing through the gas raw material cracked product quenching water system G-2 is converged with the liquid raw material cracked product passing through the liquid raw material cracked product quenching water system L-2, enters a first compression system L-4 together, and then enters a front cooling demethanization system L-5 of a liquid raw material cracked product separation route.
Example 2
The branching separation device and the separation method of the liquid raw material steam cracking product and the gas raw material steam cracking product are adopted as shown in fig. 4.
The device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system L-2, a liquid raw material cracking product quenching water system L-3, a first compression system L-4, a front cooling demethanization system L-5, an ethane removal system L-6, a carbon dioxide hydrogenation system L-7, a liquid route ethylene tower system L-8, a propane removal system L-9, a carbon three hydrogenation system L-10, a propylene tower system L-11 and a debutaning system L-12 which are sequentially connected; the liquid raw material cracking product feeding pipeline is connected with an outlet L-1 of the liquid cracking furnace; a light component discharge pipeline of the first compression system L-4 is connected with the front cold demethanizing system L-5, and a heavy component discharge pipeline of the first compression system L-4 is connected with the depropanizing system L-9; a discharging pipeline at the top of the deethanizer system L-6 is connected with a carbon dioxide hydrogenation system L-7, and a discharging pipeline at the bottom of the deethanizer system L-6 is connected with a depropanization system L-9; a tower top discharge pipeline of the depropanizing tower of the depropanizing system L-9 is sequentially connected with the carbon hydrogenation system L-10 and the propylene tower system L-11, and a tower bottom discharge pipeline of the depropanizing tower of the depropanizing system L-9 is connected with the debutanizing system L-12; the liquid route ethylene tower system L-8 is provided with a tower top ethylene discharge pipeline and a tower kettle ethane discharge pipeline; the propylene tower system L-11 is provided with a tower top propylene discharge pipeline and a tower bottom propane discharge pipeline.
The separation route of the gas raw material cracked product comprises a gas raw material cracked product feeding pipeline, a gas raw material cracked product quenching water system G-2, a second compression system G-3, a front deethanization system G-4 and a third compression system G-5; the gas raw material cracking product feeding pipeline is connected with an outlet of a gas cracking furnace G-1 and is divided into two branches, one branch is connected with a viscosity reduction tower of a quenching oil system L-2 of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system G-2 of a gas raw material cracking product; the discharge pipeline of the second compression system G-3 is connected with the front deethanization system G-4, the deethanization tower bottom discharge pipeline of the front deethanization system G-4 is connected with the depropanization system L-9, the deethanization tower top discharge pipeline of the front deethanization system G-4 is connected with the third compression system G-5, and the discharge pipeline of the third compression system G-5 is connected with the front cold demethanization system L-5.
The separation method comprises the following steps:
the liquid raw material a enters a liquid cracking furnace L-1 for steam cracking, and the obtained liquid raw material cracking product is separated by adopting the sequential flow: the liquid raw material cracked product sequentially enters a quenching oil system L-2, a quenching water system L-3 of the liquid raw material cracked product, a first compression system L-4, a front-cooling demethanization system L-5 and a deethanization system L-6; the carbon dioxide fraction obtained from the top of the deethanizer system L-6 sequentially enters the carbon dioxide hydrogenation system L-7 and the liquid route ethylene tower system L-8 to separate ethylene and recycle ethane, and the carbon three fraction obtained from the deethanizer tower kettle of the deethanizer system L-6 and the heavy component generated by the first compression system L-4 enter the depropanization system L-9; and the carbon three-fraction separated from the top of the depropanizing tower of the depropanizing system L-9 enters the carbon three-hydrogenation system L-10 for hydrogenation, then enters the propylene tower system L-11 for separating propylene and circulating propane, and the material at the bottom of the depropanizing tower of the depropanizing system L-9 enters the debutanizing system L-12.
And the gas raw material b enters a gas cracking furnace G-1 for steam cracking, and the obtained gas raw material cracking product mostly enters a gas raw material cracking product quenching water system G-2 except for removing a small amount of viscosity reduction tower viscosity reduction in a liquid raw material cracking product separation line for viscosity reduction. The gas raw material cracking product after passing through the gas raw material cracking product quenching water system G-2 enters a second compression system G-3 and then enters a front deethanization system G-4, the carbon three and above fractions separated by the front deethanization system G-4 enter a depropanization system L-9 of a liquid raw material cracking product separation route, the carbon two and below fractions separated by the front deethanization system G-4 enter a third compression system G-5 and then are converged into a front cold demethanization system L-5 of a liquid route.
Example 3
The branching separation apparatus and the separation method of the liquid raw material steam cracking product and the gaseous raw material steam cracking product as shown in fig. 5 are used.
The device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system L-2, a liquid raw material cracking product quenching water system L-3, a first compression system L-4, a front cooling demethanization system L-5, an ethane removal system L-6, a carbon dioxide hydrogenation system L-7, a liquid route ethylene tower system L-8, a propane removal system L-9, a carbon three hydrogenation system L-10, a propylene tower system L-11 and a debutaning system L-12 which are sequentially connected; the liquid raw material cracking product feeding pipeline is connected with an outlet of the liquid cracking furnace L-1; a light component discharge pipeline of the first compression system L-4 is connected with the front cold demethanizing system L-5, and a heavy component discharge pipeline of the first compression system L-4 is connected with the depropanizing system L-9; a discharging pipeline at the top of the deethanizer system L-6 is connected with a carbon dioxide hydrogenation system L-7, and a discharging pipeline at the bottom of the deethanizer system L-6 is connected with a depropanization system L-9; a tower top discharge pipeline of the depropanization system L-9 is sequentially connected with the C-C hydrogenation system L-10 and the propylene tower system L-11, and a tower bottom discharge pipeline of the depropanization system L-9 is connected with the debutanizing system L-12; the liquid route ethylene tower system L-8 is provided with a tower top ethylene discharge pipeline and a tower kettle ethane discharge pipeline; the propylene tower system L-11 is provided with a tower top propylene discharge pipeline and a tower bottom propane discharge pipeline.
The separation route of the gas raw material cracked product comprises a gas raw material cracked product feeding pipeline, a gas raw material cracked product quenching water system G-2, a second compression system G-3, a front deethanization system G-4, a third compression system G-5, a front hydrogenation system G-6 and a demethanization system G-7; the gas raw material cracking product feeding pipeline is connected with an outlet of a gas cracking furnace G-1 and is divided into two branches, one branch is connected with a viscosity reduction tower of a quenching oil system L-2 of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system G-2 of a gas raw material cracking product; the discharge pipeline of the second compression system G-3 is connected with the front deethanization system G-4, the deethanization tower bottom discharge pipeline of the front deethanization system G-4 is connected with the depropanization system L-9, the deethanization tower top discharge pipeline of the front deethanization system G-4 is connected with the third compression system G-5, the discharge pipeline of the third compression system G-5 is sequentially connected with the front hydrogenation system G-6 and the demethanization system G-7, and the discharge pipeline of the demethanization system G-7 is connected with the liquid route ethylene tower system L-8.
The separation method comprises the following steps:
the liquid raw material a enters a liquid cracking furnace L-1 for steam cracking, and the obtained liquid raw material cracking product is separated by adopting the sequential flow: the liquid raw material cracked product sequentially enters a quenching oil system L-2, a quenching water system L-3 of the liquid raw material cracked product, a first compression system L-4, a front-cooling demethanization system L-5 and a deethanization system L-6; the carbon dioxide fraction obtained from the top of the deethanizer system L-6 sequentially enters the carbon dioxide hydrogenation system L-7 and the liquid route ethylene tower system L-8 to separate ethylene and recycle ethane, and the carbon three fraction obtained from the deethanizer tower kettle of the deethanizer system L-6 and the heavy component generated by the first compression system L-4 enter the depropanization system L-9; and the carbon three-fraction separated from the top of the depropanizing tower of the depropanizing system L-9 enters the carbon three-hydrogenation system L-10 for hydrogenation, then enters the propylene tower system L-11 for separating propylene and circulating propane, and the material at the bottom of the depropanizing tower of the depropanizing system L-9 enters the debutanizing system L-12.
And the gas raw material b enters a gas cracking furnace G-1 for steam cracking, and the obtained gas raw material cracking product mostly enters a gas raw material cracking product quenching water system G-2 except for removing a small amount of viscosity reduction tower viscosity reduction in a liquid raw material cracking product separation line for viscosity reduction. The gas raw material cracking product after passing through the gas raw material cracking product quenching water system G-2 enters a second compression system G-3 and then enters a front deethanization system G-4, the carbon three and above fractions separated by the front deethanization system G-4 enter a depropanization system L-9 of a liquid raw material cracking product separation route, the carbon two and the following fractions separated by the front deethanization system G-4 sequentially enter a third compression system G-5, a front hydrogenation system G-6 and a demethanization system G-7, and the carbon two fraction separated by the demethanization system G-7 is converged into a liquid route ethylene tower system L-8.
Example 4
The branching separation apparatus and the separation method of the liquid raw material steam cleavage product and the gaseous raw material steam cleavage product as shown in fig. 6 are employed.
The device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system L-2, a liquid raw material cracking product quenching water system L-3, a first compression system L-4, a front cooling demethanization system L-5, an ethane removal system L-6, a carbon dioxide hydrogenation system L-7, a liquid route ethylene tower system L-8, a propane removal system L-9, a carbon three hydrogenation system L-10, a propylene tower system L-11 and a debutaning system L-12 which are sequentially connected; the liquid raw material cracking product feeding pipeline is connected with an outlet L-1 of the liquid cracking furnace; a light component discharge pipeline of the first compression system L-4 is connected with the front cold demethanizing system L-5, and a heavy component discharge pipeline of the first compression system L-4 is connected with the depropanizing system L-9; a discharging pipeline at the top of the deethanizer system L-6 is connected with a carbon dioxide hydrogenation system L-7, and a discharging pipeline at the bottom of the deethanizer system L-6 is connected with a depropanization system L-9; a tower top discharge pipeline of the depropanization system L-9 is sequentially connected with the C-C hydrogenation system L-10 and the propylene tower system L-11, and a tower bottom discharge pipeline of the depropanization system L-9 is connected with the debutanizing system L-12; the liquid route ethylene tower system L-8 is provided with a tower top ethylene discharge pipeline and a tower kettle ethane discharge pipeline; the propylene tower system L-11 is provided with a tower top propylene discharge pipeline and a tower bottom propane discharge pipeline.
The separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system G-2, a second compression system G-3, a front deethanization system G-4, a third compression system G-5, a front hydrogenation system G-6, a demethanization system G-7 and a gas route ethylene tower system G-8; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with the viscosity reduction tower of the quenching oil system L-2 of the liquid raw material cracking product separation route, and the other branch is connected with the quenching oil system G-2 of the gas raw material cracking product; the discharge pipeline of the second compression system G-3 is connected with the front deethanization system G-4, the deethanization tower bottom discharge pipeline of the front deethanization system G-4 is connected with the depropanization system L-9, the deethanization tower top discharge pipeline of the front deethanization system G-4 is connected with the third compression system G-5, the discharge pipeline of the third compression system G-5 is sequentially connected with the front hydrogenation system G-6 and the demethanization system G-7, the discharge pipeline of the demethanization system G-7 is connected with the gas route ethylene tower system G-8, and the gas route ethylene tower system G-8 is provided with a tower top ethylene discharge pipeline and a tower bottom ethane discharge pipeline.
The separation method comprises the following steps:
the liquid raw material a enters a liquid cracking furnace L-1 for steam cracking, and the obtained liquid raw material cracking product is separated by adopting the sequential flow: the liquid raw material cracked product sequentially enters a quenching oil system L-2, a quenching water system L-3 of the liquid raw material cracked product, a first compression system L-4, a front-cooling demethanization system L-5 and a deethanization system L-6; the carbon dioxide fraction obtained from the top of the deethanizer system L-6 sequentially enters the carbon dioxide hydrogenation system L-7 and the liquid route ethylene tower system L-8 to separate ethylene and recycle ethane, and the carbon three fraction obtained from the deethanizer tower kettle of the deethanizer system L-6 and the heavy component generated by the first compression system L-4 enter the depropanization system L-9; and the carbon three-fraction separated from the top of the depropanizing tower of the depropanizing system L-9 enters the carbon three-hydrogenation system L-10 for hydrogenation, then enters the propylene tower system L-11 for separating propylene and circulating propane, and the material at the bottom of the depropanizing tower of the depropanizing system L-9 enters the debutanizing system L-12.
And the gas raw material b enters a gas cracking furnace G-1 for steam cracking, and the obtained gas raw material cracking product mostly enters a gas raw material cracking product quenching water system G-2 except for removing a small amount of viscosity reduction tower viscosity reduction in a liquid raw material cracking product separation line for viscosity reduction. The gas raw material cracking product after passing through the gas raw material cracking product quenching water system G-2 enters a second compression system G-3 and then enters a front deethanization system G-4, the carbon three and above fractions separated by the front deethanization system G-4 enter a depropanization system L-9 of a liquid raw material cracking product separation route, the carbon two and below fractions separated by the front deethanization system G-sequentially enter a third compression system G-5, a front hydrogenation system G-6 and a demethanization system G-7, and the carbon two fraction separated by the demethanization system G-7 enters a gas route ethylene tower system G-8 to obtain ethylene and recycle ethane.
Typical distributions of the cracked products of the gaseous feed (ethane) and the liquid feed (naphtha) are shown in fig. 6, and it can be seen that the fraction content higher than three carbons in the cracked product of ethane is very small, while the propylene content in the cracked product of naphtha is high, and the cracked product of four carbons, pyrolysis gasoline, PFO, PGO and the like are also contained.
The average molecular weight of the cracked product of ethane is 23.2, the average molecular weight of the cracked product of naphtha is 31.1, and back mixing must exist when the light cracked product and the heavy cracked product are mixed and then separated, so that the separation difficulty is increased, and the energy consumption is further increased. The ethylene products are separated from the light and heavy cracking products, which is beneficial to reducing energy consumption. Although the cracking reaction is a reaction with increased volume, practice proves that the influence on the distribution of olefin in the ethane cracking product is small by increasing the pressure of the ethane furnace, so that the inlet pressure of a cracking gas compressor can be increased by increasing the pressure of the ethane furnace, and the compression power consumption is reduced. According to the process simulation calculation, the energy consumption can be reduced by about 2.1% for megaton ethylene unit separation, and the energy consumption is close to 11.5kg standard oil/ton ethylene.
The naphtha cracking product is firstly put into a quenching oil tower to get heat, and heavy components such as PFO, PGO and the like are removed, the ethane cracking product can be directly put into the quenching water tower, so that the quenching oil tower is omitted, and the ethane cracking product has higher light component (methane and hydrogen) content and larger occupied volume flow, and the light component does not enter the quenching oil tower, so that the tower diameter of the quenching oil tower can be obviously reduced. Thereby reducing the equipment investment. The cost of quenching system for megaton ethylene device can be reduced by 4500 ten thousand yuan.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. A liquid raw material steam cracking product and gas raw material steam cracking product branching separation device is characterized in that the device comprises a liquid raw material cracking product separation route and a gas raw material cracking product separation route;
the liquid raw material cracking product separation route comprises a liquid raw material cracking product feeding pipeline, a quenching oil system, a liquid raw material cracking product quenching water system, a first compression system, a front-cooling demethanizing system, an ethane removal system, a carbon dioxide hydrogenation system, a liquid route ethylene tower system, a propane removal system, a carbon three hydrogenation system, a propylene tower system and a butane removal system which are sequentially connected; the light component discharge line of the first compression system is connected with the front-cooling demethanizing system, and the heavy component discharge line of the first compression system is connected with the depropanizing system; a discharging pipeline at the top of the deethanizer system is connected with the carbon dioxide hydrogenation system, and a discharging pipeline at the bottom of the deethanizer system is connected with the depropanization system; a tower top discharge pipeline of the depropanization system is sequentially connected with the carbon three-hydrogenation system and the propylene tower system, and a tower bottom discharge pipeline of the depropanization system is connected with the debutanization system;
the separation route of the gas raw material cracking product comprises a gas raw material cracking product feeding pipeline, a gas raw material cracking product quenching water system, and an optional second compression system, a front deethanization system and a third compression system which are connected in sequence; the gas raw material cracking product feeding pipeline is divided into two branches, one branch is connected with a quenching oil system of a liquid raw material cracking product separation route, and the other branch is connected with a quenching water system of a gas raw material cracking product;
a discharge pipeline of the gas raw material cracking product quenching water system is connected with the first compression system; alternatively, the discharge line of the gaseous feed pyrolysis product quench water system is connected to the second compression system.
2. The apparatus for split-line separation of a liquid feedstock vapor cracked product and a gaseous feedstock vapor cracked product according to claim 1, wherein the discharge line of the second compression system is connected to the front end deethanization system, the deethanizer kettle discharge line of the front end deethanization system is connected to the depropanization system, the deethanizer overhead discharge line of the front end deethanization system is connected to the third compression system, and the discharge line of the third compression system is connected to the front end cold demethanizer system.
3. The split-line separation apparatus for a liquid feedstock steam cracker product and a gaseous feedstock steam cracker product of claim 2, wherein the gaseous feedstock steam cracker product separation line further includes a pre-hydrogenation system and a demethanization system, the discharge line of the third compression system is connected to the pre-hydrogenation system and the demethanization system in turn, and the discharge line of the demethanization system is connected to the liquid line ethylene column system.
4. The apparatus for the branched-line separation of a liquid feedstock vapor cracked product and a gaseous feedstock vapor cracked product of claim 3, wherein the gaseous feedstock vapor cracked product separation line further comprises a gas line ethylene column system, the output line of the demethanizer system being connected to the gas line ethylene column system.
5. The apparatus for branching off a liquid feedstock steam-cracked product and a gaseous feedstock steam-cracked product as claimed in any one of claims 1 to 4, wherein said liquid feedstock cracked product feed line is connected to a liquid cracking furnace outlet and said gaseous feedstock cracked product feed line is connected to a gas cracking furnace outlet.
6. The branching separating device of a liquid raw material steam-cracked product and a gaseous raw material steam-cracked product according to any one of claims 1 to 4, wherein,
the liquid route ethylene tower system and the gas route ethylene tower system are respectively provided with a tower top ethylene discharge pipeline and a tower bottom ethane discharge pipeline;
the propylene tower system is provided with a tower top propylene discharge pipeline and a tower bottom propane discharge pipeline;
one of the feed lines for the gaseous feed cracked product is connected to the visbreaker in the quench oil system of the liquid feed cracked product separation line.
7. A method for branching a liquid raw material steam-cracked product and a gaseous raw material steam-cracked product, which is carried out by using the branching separation apparatus for a liquid raw material steam-cracked product and a gaseous raw material steam-cracked product according to any one of claims 1 to 6, comprising the steps of:
the liquid raw material cracked product from the liquid cracking furnace sequentially enters a quenching oil system, a liquid raw material cracked product quenching water system, a first compression system, a front-cooling demethanization system and a deethanization system; the carbon dioxide fraction obtained from the top of the deethanizer system sequentially enters the carbon dioxide hydrogenation system and the liquid route ethylene tower system to separate ethylene and ethane, and the carbon three fraction obtained from the deethanizer kettle of the deethanizer system and the heavy component generated by the first compression system enter the depropanizer system; the carbon three-fraction separated from the top of the depropanizing tower of the depropanizing system enters a carbon three-hydrogenation system for hydrogenation, then enters a propylene tower system for separating propylene and propane, and the material in the bottom of the depropanizing tower of the depropanizing system enters a debutanizing system;
one part of the gas raw material cracking products from the gas cracking furnace enters a quenching oil system of a liquid raw material cracking product separation line for viscosity reduction, and the other part of the gas raw material cracking products enters a quenching water system of the gas raw material cracking products;
the gas raw material cracking product after passing through the gas raw material cracking product quenching water system is converged with the liquid raw material cracking product after passing through the liquid raw material cracking product quenching water system, and the gas raw material cracking product and the liquid raw material cracking product enter a first compression system together; or the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters a second compression system.
8. The method for the branched-path separation of a liquid feedstock steam cracking product and a gaseous feedstock steam cracking product of claim 7, wherein,
and the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters a second compression system and then enters a front deethanization system, the carbon three and above fractions separated by the front deethanization system enter the depropanization system of the liquid raw material cracking product separation route, and the carbon two and below fractions separated by the front deethanization system enter a third compression system and then are converged into a liquid route front hydrogenation system.
9. The method for the branched-path separation of a liquid feedstock steam cracking product and a gaseous feedstock steam cracking product of claim 7, wherein,
the gas raw material cracking product after passing through the gas raw material cracking product quenching water system enters a second compression system and then enters a front deethanization system, the fractions of three or more carbons separated by the front deethanization system enter the depropanization system of a liquid raw material cracking product separation route, the carbon dioxide and the fractions separated by the front deethanization system sequentially enter a third compression system, a front hydrogenation system and a demethanization system, and the carbon dioxide fraction separated by the demethanization system is converged into a liquid route ethylene tower system.
10. The method for the branched-path separation of a liquid feedstock steam cracking product and a gaseous feedstock steam cracking product of claim 7, wherein,
and the carbon two and the following fractions separated by the front deethanizing system sequentially enter a third compression system, a front hydrogenation system and a demethanizing system, and the carbon two fraction separated by the demethanizing system enters a gas route ethylene tower system to obtain ethylene and ethane.
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