CN114057534A - Catalytic cracking product separation device and separation method - Google Patents
Catalytic cracking product separation device and separation method Download PDFInfo
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- CN114057534A CN114057534A CN202010787006.3A CN202010787006A CN114057534A CN 114057534 A CN114057534 A CN 114057534A CN 202010787006 A CN202010787006 A CN 202010787006A CN 114057534 A CN114057534 A CN 114057534A
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- 238000000926 separation method Methods 0.000 title claims abstract description 96
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 71
- 238000010521 absorption reaction Methods 0.000 claims abstract description 98
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000005977 Ethylene Substances 0.000 claims abstract description 46
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000003795 desorption Methods 0.000 claims abstract description 43
- 238000005406 washing Methods 0.000 claims abstract description 38
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 33
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 33
- 229910052799 carbon Inorganic materials 0.000 claims description 90
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 89
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 30
- 239000001294 propane Substances 0.000 claims description 15
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 12
- 238000005336 cracking Methods 0.000 claims description 11
- 238000000034 method Methods 0.000 claims description 9
- 125000003118 aryl group Chemical group 0.000 claims description 6
- 238000011143 downstream manufacturing Methods 0.000 claims description 6
- 125000004122 cyclic group Chemical group 0.000 claims description 2
- 238000005504 petroleum refining Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 75
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 5
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- IYABWNGZIDDRAK-UHFFFAOYSA-N allene Chemical compound C=C=C IYABWNGZIDDRAK-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- -1 ethylene, propylene, butylene Chemical group 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
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- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
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- 238000011084 recovery Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- 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
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
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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
- C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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- Oil, Petroleum & Natural Gas (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a catalytic cracking product separation device, and belongs to the field of petroleum refining. In the device, a tower top outlet of a fractionating tower, a tower top outlet of a water washing tower, a first air compressor, a tower top outlet of a front depropanizing tower, a second air compressor, a tower top outlet of a front deethanizing tower and a first inlet of an absorption tower are communicated in sequence through pipelines; the tower bottom outlet of the front depropanizing tower is communicated with the inlet of the rear depropanizing tower, and the tower bottom outlet of the water washing tower and the tower bottom outlet of the rear depropanizing tower are both communicated with the inlet of the desorption tower through pipelines; the tower bottom outlet of the desorption tower, the tower bottom outlet of the debutanizer and the depentanizer are communicated in sequence through pipelines; the tower bottom outlet of the front deethanizer, the tower top outlet of the rear deethanizer and the inlet of the ethylene rectifying tower are communicated in sequence through pipelines; the tower bottom outlet of the front deethanizer, the tower bottom outlet of the rear deethanizer and the propylene rectifying tower are communicated in sequence through pipelines. The device can effectively separate each component in the catalytic cracking product.
Description
Technical Field
The invention relates to the field of petroleum refining, in particular to a catalytic cracking product separation device and a separation method.
Background
The catalytic cracking is a process of producing low-carbon olefins such as ethylene, propylene, butylene and the like by cracking petroleum hydrocarbons at high temperature in the presence of a catalyst, and simultaneously producing light aromatic hydrocarbons. The catalytic cracking products include: ethylene, propylene, C four, C five, light aromatic hydrocarbon, light pyrolysis oil, heavy pyrolysis oil and the like. Therefore, it is necessary to separate these different kinds of products.
The related art provides a method for recovering the carbon two components in the catalytic cracking dry gas by adopting light cold oil and middle cold oil, which is mainly used for separating the carbon two components in the catalytic cracking products.
In the process of implementing the invention, the inventor finds that at least the following problems exist in the prior art:
the related art only separates the carbon components from the catalytic cracking product, and does not give an effective separation measure for the other components in the catalytic cracking product.
Disclosure of Invention
In view of the above, the present invention provides a catalytic cracking product separation apparatus and a separation method, which can solve the above technical problems.
Specifically, the method comprises the following technical scheme:
in one aspect, there is provided a catalytic cracking product separation apparatus, the separation apparatus comprising: the system comprises a fractionating tower, a water washing tower, a first air compressor, a front depropanizing tower, a rear depropanizing tower, a desorption tower, a debutanizing tower, a depentanizing tower, a second air compressor, a front deethanizing tower, a rear deethanizing tower, a propylene rectifying tower, an ethylene rectifying tower and an absorption tower;
the top outlet of the fractionating tower, the top outlet of the water washing tower, the first air compressor, the top outlet of the front depropanizer, the second air compressor, the top outlet of the front deethanizer and the first inlet of the absorption tower are communicated in sequence through pipelines;
the tower bottom outlet of the front depropanizing tower is communicated with the inlet of the rear depropanizing tower, and the tower bottom outlet of the water washing tower and the tower bottom outlet of the rear depropanizing tower are communicated with the inlet of the desorption tower through pipelines;
the tower bottom outlet of the desorption tower, the tower bottom outlet of the debutanizer and the depentanizer are communicated in sequence through pipelines;
the tower bottom outlet of the front deethanizer, the tower top outlet of the rear deethanizer and the inlet of the ethylene rectifying tower are communicated in sequence through pipelines;
the tower bottom outlet of the front deethanizer, the tower bottom outlet of the rear deethanizer and the propylene rectifying tower are communicated in sequence through pipelines.
In one possible implementation manner, the tower bottom outlet of the absorption tower is communicated with the inlet of the desorption tower through a pipeline;
the depentanizer has a lean absorption oil outlet which is communicated with the second inlet of the absorption tower.
In a possible implementation manner, the condensate outlet of the first air compressor is communicated with the inlet of the desorption tower through a pipeline.
In one possible implementation, the catalytic cracking product separation apparatus further includes: the preprocessor is positioned between the first air compressor and the front depropanizer and is used for removing oxides, acid gas and moisture in the compressed oil gas.
On the other hand, the embodiment of the invention also provides a catalytic cracking product separation method, and any one of the catalytic cracking product separation devices is adopted in the catalytic cracking product separation method.
In one possible implementation, the separation method includes:
fractionating the catalytic cracking product by a fractionating tower to obtain heavy cracking oil, light cracking oil and a first oil-gas component through separation;
the first oil gas component enters a water washing tower from an outlet at the top of the fractionating tower for oil gas separation, and a second oil gas component at the top of the water washing tower enters a front depropanizing tower for treatment after being pressurized by a first air compressor;
the tower top component of the front depropanizing tower enters a front deethanizing tower for treatment after being pressurized by a second air compressor, the tower top component of the front deethanizing tower enters an absorption tower, the carbon three components are recovered from the lean absorption oil, and the tower top dry gas of the absorption tower is sent to a downstream processing device; the tower bottom component of the front deethanizer enters a rear deethanizer for separation, and the tower top carbon two component of the rear deethanizer enters an ethylene rectifying tower to complete the separation of ethylene and ethane; the three components of the bottom carbon of the post-deethanizer enter a propylene rectifying tower to complete the separation of propylene and propane;
the tower bottom components of the front depropanizing tower enter a rear depropanizing tower to separate the carbon three components and the carbon four components, and the tower bottom components of the rear depropanizing tower and the tower bottom components of the water washing tower sequentially pass through a desorption tower, a debutanizing tower and a depentanizing tower to complete the separation of the mixed carbon four components, the carbon five components and the lean absorption oil.
In one possible implementation, the separation method includes:
the rich absorption oil at the bottom of the absorption tower passes through a desorption tower, a debutanizer and a depentanizer in sequence to be regenerated to obtain lean absorption oil;
and the lean absorption oil enters the absorption tower for cyclic utilization.
In one possible implementation, the lean absorption oil is an aromatic gasoline.
In a possible implementation mode, the interstage condensate of the first air compressor passes through the desorption tower, the debutanizer and the depentanizer along with the tower bottom component of the post depropanizer and the tower bottom component of the water washing tower, and separation of mixed carbon four component, carbon five component and lean absorption oil is completed.
In a possible implementation mode, after a second oil gas component on the top of the water washing tower is pressurized by a first air compressor, oxides, acid gas and water in the second oil gas component are removed by a preprocessor, and then the second oil gas component enters a front depropanizing tower for treatment;
the preprocessor is positioned between the first air compressor and the front depropanizing tower and is used for removing oxides, acid gas and moisture in the compressed oil gas.
The technical scheme provided by the embodiment of the invention has the beneficial effects that at least:
according to the catalytic cracking product separation device provided by the embodiment of the invention, the top outlet of the fractionating tower, the top outlet of the water washing tower, the first air compressor, the top outlet of the front depropanizing tower, the second air compressor, the top outlet of the front deethanizing tower and the first inlet of the absorption tower are sequentially communicated through pipelines, so that the non-clear separation of carbon two and carbon three can be realized; the clear separation of the carbon three and the carbon four components is completed by communicating the tower bottom outlet of the front depropanizing tower with the inlet of the rear depropanizing tower; the separation of ethylene and ethane is completed by sequentially communicating the tower bottom outlet of the front deethanizer, the tower top outlet of the rear deethanizer and the inlet of the ethylene rectifying tower through pipelines; the separation of propylene and propane is completed by sequentially communicating the tower bottom outlet of the front deethanizer, the tower bottom outlet of the rear deethanizer and the propylene rectifying tower through pipelines; the tower bottom outlet of the water washing tower and the tower bottom outlet of the post depropanizing tower are communicated with the inlet of the desorption tower through pipelines, and the tower bottom outlet of the desorption tower, the tower bottom outlet of the debutanizing tower and the depentanizing tower are communicated in sequence through pipelines, so that the separation of the mixed carbon four component, the carbon five component and the lean absorption oil is completed. Thus, the device provided by the embodiment of the invention can be used for effectively separating each component in the catalytic cracking product.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a catalytic cracking product separation device provided in an embodiment of the present invention.
The reference numerals denote:
1-a fractionating tower, 2-a water washing tower, 3-a first air compressor, 4-a front depropanizing tower,
5-post depropanizer, 6-desorber, 7-debutanizer, 8-depentanizer,
9-a second gas compressor, 10-a front deethanizer, 11-a rear deethanizer,
12-propylene rectifying tower, 13-ethylene rectifying tower, 14-absorption tower and 15-preprocessor.
Detailed Description
In order to make the technical solutions and advantages of the present invention clearer, the following will describe embodiments of the present invention in further detail with reference to the accompanying drawings.
In one aspect, an embodiment of the present invention provides a catalytic cracking product separation apparatus, as shown in fig. 1, the catalytic cracking product separation apparatus including: the system comprises a fractionating tower 1, a water washing tower 2, a first air compressor 3, a front depropanizing tower 4, a rear depropanizing tower 5, a desorption tower 6, a debutanizing tower 7, a depentanizing tower 8, a second air compressor 9, a front deethanizing tower 10, a rear deethanizing tower 11, a propylene rectifying tower 12, an ethylene rectifying tower 13 and an absorption tower 14.
Wherein, the top outlet of the fractionating tower 1, the top outlet of the water washing tower 2, the first air compressor 3, the top outlet of the front depropanizing tower 4, the second air compressor 9, the top outlet of the front deethanizing tower 10 and the first inlet (namely, the raw material inlet) of the absorption tower 14 are communicated in sequence through pipelines.
The outlet at the bottom of the front depropanizing tower 4 is communicated with the inlet of the rear depropanizing tower 5, and the outlet at the bottom of the water washing tower 2 and the outlet at the bottom of the rear depropanizing tower 5 are communicated with the inlet of the desorption tower 6 through pipelines.
The tower bottom outlet of the desorption tower 6, the tower bottom outlet of the debutanizer 7 and the depentanizer 8 are communicated in sequence through pipelines.
The tower bottom outlet of the front deethanizer 10, the tower top outlet of the rear deethanizer 11, and the inlet of the ethylene rectifying tower 13 are communicated in sequence through pipelines.
The tower bottom outlet of the front deethanizer 10, the tower bottom outlet of the rear deethanizer 11, and the propylene rectifying tower 12 are communicated in sequence through pipelines.
The working principle of the catalytic cracking product separation device provided by the embodiment of the invention is described as follows:
the catalytic cracking product is fractionated by a fractionating tower 1, heavy cracking oil is separated from the bottom of the fractionating tower 1, light cracking oil is separated from the middle of the fractionating tower 1, and a first oil gas component is separated from the top of the fractionating tower 1. The first oil gas component enters a water washing tower 2 from the outlet of the tower top of a fractionating tower 1 for oil-gas separation, the second oil gas component in the first oil gas component, mainly gasoline and steam condensate water, is separated and respectively pumped out at the bottom of the water washing tower 2, and the second oil gas component at the tower top of the water washing tower 2 enters a front depropanizing tower 4 for treatment after being pressurized by a first air compressor 3. The tower top components of the front depropanizing tower 4 enter a front deethanizing tower 10 for treatment after being pressurized by a second air compressor 9, the tower top components of the front deethanizing tower 10 enter an absorption tower 14, the three components of carbon are recovered from the lean absorption oil in the absorption tower 14, and the tower top dry gas of the absorption tower 14 is sent to a downstream processing device. The tower bottom components of the front deethanizer 10 enter a rear deethanizer 11 for separation, and the tower top carbon components of the rear deethanizer 11 enter an ethylene rectifying tower 13 to complete the separation of ethylene and ethane; and the three components of the bottom carbon of the post-deethanizer 11 enter a propylene rectifying tower 12 to complete the separation of propylene and propane.
The tower bottom components of the front depropanizing tower 4 enter the rear depropanizing tower 5 to separate the carbon three components and the carbon four components, after all the oil gas at the tower top of the rear depropanizing tower 5 is condensed and cooled, one part of the oil gas is returned to the tower top of the rear depropanizing tower 5 as cold reflux, and the other part of the oil gas is returned to the tower top of the front depropanizing tower 4. The tower bottom components of the post depropanizing tower 5 and the tower bottom components of the water washing tower 2 sequentially pass through a desorption tower 6, a debutanizing tower 7 and a depentanizing tower 8 to complete the separation of the mixed carbon four component, the carbon five component and the lean absorption oil. Wherein, the mixed carbon four component is extracted from the debutanizer 7, and the carbon five component and the lean absorption oil are respectively extracted from different positions of the depentanizer 8.
It can be seen that the catalytic cracking product separation device provided by the embodiment of the present invention can realize the unclear separation of carbon two and carbon three by sequentially communicating the top outlet of the fractionating tower 1, the top outlet of the water scrubber 2, the top outlet of the first air compressor 3, the top outlet of the front depropanizing tower 4, the second air compressor 9, the top outlet of the front deethanizing tower 10, and the first inlet of the absorption tower 14 through pipelines; the clear separation of the carbon three and the carbon four components is completed by communicating the tower bottom outlet of the front depropanizing tower 4 with the inlet of the rear depropanizing tower 5; the separation of ethylene and ethane is completed by sequentially communicating the tower bottom outlet of the front deethanizer 10, the tower top outlet of the rear deethanizer 11, and the inlet of the ethylene rectifying tower 13 through pipelines; the separation of propylene and propane is completed by sequentially communicating the bottom outlet of the front deethanizer 10, the bottom outlet of the rear deethanizer 11, and the propylene rectification column 12 through pipelines; the tower bottom outlet of the water washing tower 2 and the tower bottom outlet of the post depropanizing tower 5 are communicated with the inlet of the desorption tower 6 through pipelines, and the tower bottom outlet of the desorption tower 6, the tower bottom outlet of the debutanizing tower 7 and the depentanizing tower 8 are communicated in sequence through pipelines, so that the separation of the mixed carbon four component, the carbon five component and the lean absorption oil is completed. Thus, the device provided by the embodiment of the invention can be used for effectively separating each component in the catalytic cracking product.
Further, as shown in fig. 1, in the catalytic cracking product separation apparatus provided in the embodiment of the present invention, the outlet of the bottom of the absorption tower 14 is communicated with the inlet of the desorption tower 6 through a pipeline; the depentanizer 8 has a lean absorption oil outlet in communication with a second inlet of the absorber 14.
The tower top components of the front deethanizer 10 enter an absorption tower 14, the carbon three components are recovered from the lean absorption oil in the absorption tower 14, the tower top dry gas of the absorption tower 14 is sent to a downstream processing device, and the lean absorption oil absorbing the carbon three components in the absorption tower 14 becomes rich absorption oil. Because the outlet at the bottom of the absorption tower 14 is communicated with the inlet of the desorption tower 6 through a pipeline, the rich absorption oil at the bottom of the absorption tower 14 passes through the desorption tower 6, the debutanizer 7 and the depentanizer 8 in sequence to be regenerated to obtain the lean absorption oil, and simultaneously, the carbon three components in the lean absorption oil are further separated. Because the lean absorption oil outlet of the depentanizer 8 is communicated with the second inlet of the absorption tower 14, the lean absorption oil enters the absorption tower 14 and can be recycled.
In the embodiment of the invention, the lean absorption oil is aromatic gasoline.
Further, as shown in fig. 1, in the catalytic cracking product separation apparatus provided in the embodiment of the present invention, the condensate outlet of the first air compressor 3 is communicated with the inlet of the desorption tower 6 through a pipeline.
Therefore, the interstage condensate of the first air compressor 3 passes through the tower bottom component of the depropanizing tower 5 and the tower bottom component of the water washing tower 2 together through the desorption tower 6, the debutanizing tower 7 and the depentanizing tower 8, so that the separation of the mixed carbon four component, the carbon five component and the lean absorption oil is completed, and the recovery efficiency is improved.
Further, as shown in fig. 1, the catalytic cracking product separation apparatus provided by the embodiment of the present invention further includes: a pretreater 15, the pretreater 15 is located between the first gas compressor 3 and the front depropanizer 4 for removing the oxides, acid gases and moisture from the compressed oil gas, i.e. the second oil gas component.
Through the arrangement, before the second oil gas component enters the front depropanizing tower 4, oxides, acid gas and moisture in the second oil gas component are removed by the preprocessor 15, so that the subsequent separation efficiency is improved.
Based on any one of the catalytic cracking product separation devices, the embodiment of the invention also provides a catalytic cracking product separation method, and the catalytic cracking product separation method adopts any one of the catalytic cracking product separation devices.
In one possible implementation manner, an embodiment of the present invention provides a separation method for a catalytic cracking product, where the separation method includes:
the catalytic cracking product is fractionated in a fractionating tower 1, and heavy cracking oil, light cracking oil and a first oil gas component are obtained through separation.
The top outlet of the fractionating tower 1, the top outlet of the water washing tower 2, the first air compressor 3, the top outlet of the front depropanizing tower 4, the second air compressor 9, the top outlet of the front deethanizing tower 10 and the first inlet (i.e. raw material inlet) of the absorption tower 14 are communicated in sequence through pipelines.
Thus, the first oil gas component enters the water scrubber 2 from the outlet of the tower top of the fractionating tower 1 for oil gas separation, and the second oil gas component at the tower top of the water scrubber 2 enters the front depropanizing tower 4 for treatment after being pressurized by the first air compressor 3; the tower top component of the front depropanizing tower 4 enters a front deethanizing tower 10 for treatment after being pressurized by a second air compressor 9, the tower top component of the front deethanizing tower 10 enters an absorption tower 14, the carbon three components are recovered from the lean absorption oil, and the tower top dry gas of the absorption tower 14 is sent to a downstream processing device.
Wherein, the second oil gas component at the top of the water scrubber 2 is pressurized to 1.0MPa-2.0MPa by the first air compressor 3. The tower top component of the front depropanizing tower 4 is pressurized to 2.0-4.0 Mpa by the second gas compressor 9 to obtain high separation efficiency.
The tower bottom outlet of the front depropanizing tower 4 is communicated with the inlet of the rear depropanizing tower 5, the tower bottom outlet of the water washing tower 2 and the tower bottom outlet of the rear depropanizing tower 5 are communicated with the inlet of the desorption tower 6 through pipelines, and the tower bottom outlet of the desorption tower 6, the tower bottom outlet of the debutanizing tower 7 and the depentanizing tower 8 are communicated in sequence through pipelines. Thus, the tower bottom component of the front depropanizing tower 4 enters the rear depropanizing tower 5 to separate the carbon three component and the carbon four component, and the tower bottom component of the rear depropanizing tower 5 and the tower bottom component of the water washing tower 2 sequentially pass through the desorption tower 6, the debutanizer 7 and the depentanizer 8 to complete the separation of the mixed carbon four component, the carbon five component and the lean absorption oil.
Because the tower bottom outlet of the front deethanizer 10, the tower top outlet of the rear deethanizer 11 and the inlet of the ethylene rectifying tower 13 are communicated in sequence through pipelines, and the tower bottom outlet of the front deethanizer 10, the tower bottom outlet of the rear deethanizer 11 and the propylene rectifying tower 12 are communicated in sequence through pipelines, thus, the tower bottom components of the front deethanizer 10 enter the rear deethanizer 11 for separation, and the tower top carbon two components of the rear deethanizer 11 enter the ethylene rectifying tower 13, thereby completing the separation of ethylene and ethane; and the three components of the bottom carbon of the post-deethanizer 11 enter a propylene rectifying tower 12 to complete the separation of propylene and propane.
Therefore, the device provided by the embodiment of the invention can be used for effectively separating each component in the catalytic cracking product.
Further, in the catalytic cracking product separation device provided by the embodiment of the invention, the outlet at the bottom of the absorption tower 14 is communicated with the inlet of the desorption tower 6 through a pipeline; the depentanizer 8 has a lean absorption oil outlet in communication with a second inlet of the absorber 14.
Thus, the method for separating catalytic cracking products provided by the embodiment of the invention further comprises the following steps: rich absorption oil at the bottom of the absorption tower 14 passes through a desorption tower 6, a debutanizer 7 and a depentanizer 8 in sequence, and poor absorption oil is obtained through regeneration; the lean absorption oil enters the absorption tower 14 for recycling.
As one example, the lean absorption oil is an aromatic gasoline.
In the embodiment of the invention, the dosage of the aromatic hydrocarbon gasoline is adjusted according to the content requirement of a downstream processing device on the carbon three-component in the dry gas at the top of the absorption tower 14, and the rich absorption oil at the bottom of the absorption tower 14 returns to the desorption tower 6, the debutanizer 7 and the depentanizer 8 for regeneration.
Wherein the temperature of the lean absorption oil entering the absorption tower 14 is higher than-40 ℃, and two, three or more intercoolers can be arranged in the absorption tower 14, and the cold temperature of the intercoolers is higher than-40 ℃ to ensure that a good absorption effect is obtained.
Because the condensate outlet of the first air compressor 3 is communicated with the inlet of the desorption tower 6 through a pipeline, the interstage condensate of the first air compressor 3 then passes through the tower bottom component of the depropanizing tower 5 and the tower bottom component of the water washing tower 2 together to pass through the desorption tower 6, the debutanizer 7 and the depentanizer 8, and the separation of the mixed carbon four component, the carbon five component and the lean absorption oil is completed together.
In a possible implementation manner, after the second oil gas component at the top of the water scrubber 2 is pressurized by the first air compressor 3, the oxide, the acid gas and the moisture in the second oil gas component are removed by the preprocessor 15, and then the second oil gas component enters the front depropanizing tower 4 to be processed, wherein the preprocessor 15 is located between the first air compressor 3 and the front depropanizing tower 4 and is used for removing the oxide, the acid gas and the moisture in the compressed oil gas.
In the embodiment of the invention, the operating pressure range of the front depropanizing tower 4 is 1.0-2.0 Mpa, and the volume content of the components with four or more carbon in the oil gas component at the top of the front depropanizing tower 4 is 0-5%.
In the present example, the operating pressure of the post-depropanizer 5 was in the range of 0.4 Mpa0.8Mpa.
The mixed carbon four component is separated by a debutanizer 7, wherein the mixed carbon four component can be directly returned to the catalytic cracking reactor for recycling, or the mixed carbon four component can be returned to the catalytic cracking reactor for recycling after butadiene is removed.
The carbon five components are separated by the depentanizer 8, wherein the carbon five components can be completely returned to the catalytic cracking reactor for remixing, or part of the carbon five components can be returned to the catalytic cracking reactor for remixing.
In the embodiment of the invention, the overhead stream of the post-deethanization is the overhead carbon two component, wherein the overhead carbon two component is divided into three parts, one part enters the top of the post-deethanization tower 11 as cold reflux, one part returns to the top of the front deethanization tower 10 as cold reflux, and the other part enters the ethylene rectifying tower 13. Wherein the amount of overhead carbon components entering the ethylene rectification column 13 is determined by the downstream plant processing load. The amount of the high-purity ethylene obtained by the ethylene rectifying tower 13 is 90-98% of the total amount of the ethylene obtained by catalytic cracking reaction.
If acetylene is contained in the tower top carbon dioxide component of the post-deethanizer 11, the acetylene needs to be removed and then enters the ethylene rectifying tower 13;
if the carbon three components at the bottom of the post-deethanizer 11 contain impurities such as methylacetylene or propadiene, the impurities such as methylacetylene or propadiene in the carbon three components at the bottom of the post-deethanizer need to be removed and then enter the propylene rectifying tower 12.
In one possible implementation, the ethane separated from the bottom of the ethylene rectification column 13 can be returned as cold reflux to the top of the front end deethanizer.
In a possible implementation mode, ethane separated from the bottom of the ethylene rectifying tower 13 can be taken out of the device as a product and can also be totally or partially returned to the catalytic cracking reactor for recycling.
In one possible implementation, propane separated from the bottom of the propylene rectification column 12 may be returned to the top of the front deethanizer 10 as a cold reflux.
In a possible implementation mode, the propane separated from the bottom of the propylene rectifying tower 12 can be taken out of the device as a product and can also be totally or partially returned to the catalytic cracking reactor for recycling.
Based on the above, the embodiment of the present invention provides a method for separating a catalytic cracking reaction product, which includes the following steps:
the reaction oil gas comes from the catalytic cracking reactor and enters the bottom of the fractionating tower 1, and heavy cracking oil and light cracking oil are separated from bottom to top. The tower top oil gas of the fractionating tower 1 enters a water washing tower 2, is in countercurrent contact with circulating water for cooling, and crude gasoline and water which are condensed are settled and separated in a tower kettle and are respectively pumped out. The oil gas at the top of the water washing tower 2 enters a first air compressor 3 to be pressurized to 1.0-2.0 Mpa, and pretreatment such as oxide removal, acid gas removal, water removal and the like is carried out.
The pretreated compressed oil gas is sent to a front depropanizing tower 4, the operation is carried out under the pressure of 1.0Mpa-2.0Mpa, the volume content of carbon four and more components in the oil gas at the tower top of the tower is controlled to be 0-5 percent, and the material flow at the tower bottom is sent to a rear depropanizing tower 5 to carry out the clear separation of carbon three and carbon four components. The operating pressure range of the post-depropanizing tower 5 is 0.4Mpa-0.8Mpa, and the volume content of the carbon three and the following components in the tower bottom stream of the post-depropanizing tower is controlled to be 0 percent to 3 percent.
The tower bottom material flow of the post depropanizing tower 5, the tower bottom crude gasoline of the water washing tower 2 and the gas compressor interstage condensate are sent to a desorption tower 6 to remove light components with the carbon number of three or less, and then enter a debutanizer 7 and a depentanizer 8, and the mixed carbon four and carbon five components and the aromatic gasoline are separated out in sequence. Wherein, after butadiene is separated from the mixed C4, part or all of the butadiene can be returned to the catalytic cracking reactor for refining, and part or all of the C five components can be returned to the catalytic cracking reactor for refining.
The oil gas at the top of the front depropanizing tower 4 is further pressurized to 2.0-4.0 Mpa by a second air compressor 9, and then is sent to a front deethanizing tower 10, and the volume content of light components such as methane in the tower bottom material flow of the tower is controlled to be 0-3 percent. The overhead gas of the front deethanizer 10 enters an absorption tower 14, aromatic hydrocarbon gasoline cooled to a temperature higher than minus 40 ℃ is used as an absorbent, two or three intercoolers are arranged, the temperature of the intercoolers after cooling is higher than minus 40 ℃, and the volume content of the top carbon three components of the absorption tower 14 is controlled to be 0-3%. The ethylene-containing dry gas at the top of the absorber column 14 is sent to a subsequent processing unit. The rich absorption oil at the bottom of the absorption tower 14 is sent to the desorption tower 6, and is regenerated by removing light components through the debutanizer 7 and the depentanizer 8, and then returns to the absorption tower 14 for recycling.
The bottom material flow of the front deethanizer 10 enters a rear deethanizer 11 to finish the separation of carbon and carbon, the top material flow of the rear deethanizer 11 is divided into three parts, one part of the top material flow enters the top of the rear deethanizer 11 as cold reflux, one part of the top material flow returns to the top of the front deethanizer 10 as cold reflux, and the other part of the top material flow enters an ethylene rectifying tower 13 to finish the separation of ethylene and ethane, so as to obtain ethylene and ethane products with required concentration.
The bottom material flow of the post-deethanizer 11 enters a propylene rectifying tower 12 to complete the separation of propylene and propane, and propylene and propane products with required concentration are obtained. The ethylene and the propylene are taken as product delivery devices, and the ethane and the propane can be taken as the product delivery devices, can also be returned to the catalytic cracking reactor for recycling, and can also be returned to the tower top of the front deethanizer 10 to be taken as the tower top cold reflux of the tower.
If the overhead material flow of the post-deethanizer 11 contains acetylene, the acetylene needs to be removed and then enters an ethylene rectifying tower 13; if the bottom stream of the post-deethanizer 11 contains impurities such as methylacetylene or propadiene, the bottom stream needs to be removed and then enters the propylene rectifying tower 12.
Therefore, the process can realize the high-efficiency separation of the catalytic cracking reaction products. Wherein one part of the ethylene is sent to a downstream device in the form of ethylene-containing dry gas, such as a device for preparing ethylbenzene from the dry gas for further processing, and the other part of the ethylene is sent to the downstream device for processing in the form of high-purity ethylene or is sold as a product, thereby realizing the flexible treatment of different grades of products. The ethane, propane, mixed carbon four and carbon five components obtained by separation in the process can be sold as products and can also be returned to a catalytic cracking reactor for remilling, so that the yield of the target products ethylene and propylene is improved. The embodiment of the invention does not adopt cryogenic separation related equipment, reduces equipment investment, and has the advantages of lower energy consumption, simple operation and maintenance, safety and reliability.
The invention is further described below by means of specific examples:
the composition (dry basis) of oil gas at the outlet of a reactor of a certain catalytic cracking unit is shown in table 1, and the separation process is shown in attached figure 1.
TABLE 1
| Components | Mass fraction of% | Mass flow, kg/h |
| Dry gas | 28.51 | 54978 |
| Liquefied gas | 23.63 | 45560 |
| Gasoline component | 16.73 | 32266 |
| Light pyrolysis oil | 20.26 | 39074 |
| Heavy pyrolysis oil | 10.86 | 20948 |
| Total up to | 100 | 192826 |
| Wherein ethylene | 16.59 | 31995 |
| Wherein propylene is | 13.16 | 25382 |
The oil gas from the catalytic cracking reactor enters the bottom of the fractionating tower 1, and the heavy cracked oil and the light cracked oil are separated from bottom to top. The tower top oil gas of the fractionating tower 1 enters a water washing tower 2, is in countercurrent contact with circulating water for cooling, and crude gasoline and water which are condensed are settled and separated in a tower kettle and are respectively pumped out. The oil gas at the top of the water scrubber 2 enters a first air compressor 3, is compressed and pressurized to 1.6Mpa by three stages, and is pretreated to remove oxides, acid gas, water and the like.
The pretreated compressed oil gas is sent to a front depropanizing tower 4, the operation is carried out under the pressure of 1.5Mpa, the volume content of carbon four and more components in the oil gas at the tower top of the tower is controlled to be 0.025 percent, and the product flow at the tower bottom is sent to a rear depropanizing tower 5 to carry out the clear separation of carbon three and carbon four components. The operation pressure of the post-depropanizing tower 5 is 0.7Mpa, and the volume content of carbon three and the following components in the tower bottom flow of the post-depropanizing tower is controlled to be 0.2 percent.
The tower bottom material flow of the post depropanizing tower 5, the tower bottom crude gasoline of the water washing tower 2 and the gas compressor interstage condensate are sent to a desorption tower 6 to remove light components with the carbon number of three or less, and then enter a debutanizer 7 and a depentanizer 8, and the mixed carbon four and carbon five components and the aromatic gasoline are separated out in sequence. Wherein, the mixed C four is separated out butadiene and then all returns to the catalytic cracking reactor for remixing, and the C five components are all returned to the catalytic cracking reactor for remixing.
The oil gas at the top of the front depropanizing tower 4 is further pressurized to 2.4Mpa by a second gas compressor 9 and then sent to a front deethanizing tower 10, and the volume content of light components such as methane in the tower bottom material flow of the front deethanizing tower is controlled to be 0.05 percent. The overhead gas of the front deethanizer 10 enters an absorption tower 14, aromatic hydrocarbon gasoline cooled to minus 25 ℃ is used as an absorbent, two intercoolers are arranged, the temperature of the intercoolers after cooling is minus 25 ℃, and the volume content of the top carbon three components of the absorption tower 14 is controlled to be 1.0%. The dry gas with the ethylene volume fraction of 37.7 percent at the tower top of the absorption tower 14 is sent to a device for preparing ethylbenzene from the dry gas. The rich absorption oil at the bottom of the absorption tower 14 is sent to the desorption tower 6, and is regenerated by removing light components through the debutanizer 7 and the depentanizer 8, and then returns to the absorption tower 14 for recycling.
The bottom material flow of the front deethanizer 10 enters the rear deethanizer 11 to finish the separation of carbon and carbon, the mixed carbon material flow at the top of the rear deethanizer 11 is divided into three parts, one part enters the top of the rear deethanizer 11 as cold reflux, one part returns to the top of the front deethanizer 10 as cold reflux, the other part enters the hydrogenation reactor, and the ethylene is sent to the ethylene rectifying tower 13 after acetylene is removed. 8500kg/h of ethylene product with the volume fraction of 99.99 percent is extracted from the top of the ethylene rectifying tower 13, and ethane with the volume fraction of 98 percent is obtained from the bottom of the tower and is sent to a catalytic cracking reactor for recycling.
And the bottom material flow of the post-deethanizer 11 enters a dealkynization reactor, after methyl acetylene and propadiene are removed, the bottom material flow is sent to a propylene rectifying tower 12 to complete the separation of propylene and propane, a propylene product with the volume fraction of 99.6 percent is obtained at the tower top of the tower, propane with the volume fraction of 95 percent is obtained at the tower bottom of the tower, and the propane is sent to a catalytic cracking reactor for recycling.
The above description is only for facilitating the understanding of the technical solutions of the present invention by those skilled in the art, and is not intended to limit the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A catalytic cracking product separation apparatus, characterized in that the separation apparatus comprises: the system comprises a fractionating tower, a water washing tower, a first air compressor, a front depropanizing tower, a rear depropanizing tower, a desorption tower, a debutanizing tower, a depentanizing tower, a second air compressor, a front deethanizing tower, a rear deethanizing tower, a propylene rectifying tower, an ethylene rectifying tower and an absorption tower;
the top outlet of the fractionating tower, the top outlet of the water washing tower, the first air compressor, the top outlet of the front depropanizer, the second air compressor, the top outlet of the front deethanizer and the first inlet of the absorption tower are communicated in sequence through pipelines;
the tower bottom outlet of the front depropanizing tower is communicated with the inlet of the rear depropanizing tower, and the tower bottom outlet of the water washing tower and the tower bottom outlet of the rear depropanizing tower are communicated with the inlet of the desorption tower through pipelines;
the tower bottom outlet of the desorption tower, the tower bottom outlet of the debutanizer and the depentanizer are communicated in sequence through pipelines;
the tower bottom outlet of the front deethanizer, the tower top outlet of the rear deethanizer and the inlet of the ethylene rectifying tower are communicated in sequence through pipelines;
the tower bottom outlet of the front deethanizer, the tower bottom outlet of the rear deethanizer and the propylene rectifying tower are communicated in sequence through pipelines.
2. The catalytic cracking product-separating apparatus according to claim 1, wherein the bottom outlet of the absorption column is communicated with the inlet of the desorption column through a line;
the depentanizer has a lean absorption oil outlet which is communicated with the second inlet of the absorption tower.
3. The catalytic cracking product separation device of claim 1, wherein the condensate outlet of the first air compressor is communicated with the inlet of the desorption tower through a pipeline.
4. The catalytic cracking product separation apparatus according to claim 1, further comprising: the preprocessor is positioned between the first air compressor and the front depropanizer and is used for removing oxides, acid gas and moisture in the compressed oil gas.
5. A method for separating a catalytic cracking product, characterized by using the catalytic cracking product separation apparatus according to any one of claims 1 to 4.
6. The catalytic cracking product separation method according to claim 5, wherein the separation method comprises:
fractionating the catalytic cracking product by a fractionating tower to obtain heavy cracking oil, light cracking oil and a first oil-gas component through separation;
the first oil gas component enters a water washing tower from an outlet at the top of the fractionating tower for oil gas separation, and a second oil gas component at the top of the water washing tower enters a front depropanizing tower for treatment after being pressurized by a first air compressor;
the tower top component of the front depropanizing tower enters a front deethanizing tower for treatment after being pressurized by a second air compressor, the tower top component of the front deethanizing tower enters an absorption tower, the carbon three components are recovered from the lean absorption oil, and the tower top dry gas of the absorption tower is sent to a downstream processing device; the tower bottom component of the front deethanizer enters a rear deethanizer for separation, and the tower top carbon two component of the rear deethanizer enters an ethylene rectifying tower to complete the separation of ethylene and ethane; the three components of the bottom carbon of the post-deethanizer enter a propylene rectifying tower to complete the separation of propylene and propane;
the tower bottom components of the front depropanizing tower enter a rear depropanizing tower to separate the carbon three components and the carbon four components, and the tower bottom components of the rear depropanizing tower and the tower bottom components of the water washing tower sequentially pass through a desorption tower, a debutanizing tower and a depentanizing tower to complete the separation of the mixed carbon four components, the carbon five components and the lean absorption oil.
7. The catalytic cracking product separation method according to claim 6, wherein the separation method comprises:
the rich absorption oil at the bottom of the absorption tower passes through a desorption tower, a debutanizer and a depentanizer in sequence to be regenerated to obtain lean absorption oil;
and the lean absorption oil enters the absorption tower for cyclic utilization.
8. The catalytic cracking product separation process of claim 7, wherein the lean absorption oil is aromatic gasoline.
9. The separation method of catalytic cracking products according to claim 6, characterized in that the interstage condensate of the first air compressor passes through the desorption tower, the debutanizer and the depentanizer along with the tower bottom component of the post depropanizer and the tower bottom component of the water washing tower, and the separation of mixed C-IV component, C-V component and lean absorption oil is completed.
10. The catalytic cracking product separation method of claim 6, wherein the second oil gas component at the top of the water scrubber is pressurized by the first air compressor, then is subjected to oxide, acid gas and water removal by the preprocessor, and then enters the front depropanizing tower for treatment;
the preprocessor is positioned between the first air compressor and the front depropanizing tower and is used for removing oxides, acid gas and moisture in the compressed oil gas.
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