CN109678635A - A kind of utilization method of saturated hydrocarbons cracking gas separating system and rich ethane/propane saturated hydrocarbons - Google Patents
A kind of utilization method of saturated hydrocarbons cracking gas separating system and rich ethane/propane saturated hydrocarbons Download PDFInfo
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- CN109678635A CN109678635A CN201710979287.0A CN201710979287A CN109678635A CN 109678635 A CN109678635 A CN 109678635A CN 201710979287 A CN201710979287 A CN 201710979287A CN 109678635 A CN109678635 A CN 109678635A
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000005336 cracking Methods 0.000 title claims abstract description 66
- 229930195734 saturated hydrocarbon Natural products 0.000 title claims abstract description 46
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000001294 propane Substances 0.000 title claims abstract description 33
- 239000007789 gas Substances 0.000 claims abstract description 116
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000005977 Ethylene Substances 0.000 claims abstract description 80
- 238000010521 absorption reaction Methods 0.000 claims abstract description 70
- 238000003795 desorption Methods 0.000 claims abstract description 45
- 238000010791 quenching Methods 0.000 claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000000605 extraction Methods 0.000 claims abstract description 22
- 239000002918 waste heat Substances 0.000 claims abstract description 18
- 238000001035 drying Methods 0.000 claims abstract description 17
- 230000000171 quenching effect Effects 0.000 claims abstract description 15
- 229920000642 polymer Polymers 0.000 claims abstract description 11
- 230000008569 process Effects 0.000 claims abstract description 11
- 238000000197 pyrolysis Methods 0.000 claims abstract description 11
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 9
- 230000009102 absorption Effects 0.000 claims description 66
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 65
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 65
- 238000005984 hydrogenation reaction Methods 0.000 claims description 39
- 230000009103 reabsorption Effects 0.000 claims description 39
- 239000003502 gasoline Substances 0.000 claims description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 36
- 229910052799 carbon Inorganic materials 0.000 claims description 36
- 239000000463 material Substances 0.000 claims description 29
- 238000000926 separation method Methods 0.000 claims description 25
- 239000002250 absorbent Substances 0.000 claims description 24
- 230000002745 absorbent Effects 0.000 claims description 24
- 239000003381 stabilizer Substances 0.000 claims description 23
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 22
- 239000000203 mixture Substances 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 11
- 239000001569 carbon dioxide Substances 0.000 claims description 11
- 239000002253 acid Substances 0.000 claims description 9
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 9
- 239000002904 solvent Substances 0.000 claims description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 8
- 238000007670 refining Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 6
- 150000001345 alkine derivatives Chemical class 0.000 claims description 6
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 5
- -1 acetylene hydrocarbon Chemical class 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 claims description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 4
- 150000001993 dienes Chemical class 0.000 claims description 3
- 239000001282 iso-butane Substances 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 2
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 abstract description 5
- 238000004821 distillation Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 49
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 22
- 239000003921 oil Substances 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 230000000153 supplemental effect Effects 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 230000000087 stabilizing effect Effects 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 4
- 238000004227 thermal cracking Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 150000001361 allenes Chemical class 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 238000004517 catalytic hydrocracking Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004230 steam cracking Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- MWWATHDPGQKSAR-UHFFFAOYSA-N propyne Chemical compound CC#C MWWATHDPGQKSAR-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- 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
-
- 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
-
- 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
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to refineries to be saturated utilization of resources field, be related to the utilization method of a kind of saturated hydrocarbons cracking gas separating system and rich ethane/propane saturated hydrocarbons.It includes: pyrolysis furnace, waste heat boiler, quenching water column, compressor, absorption tower, desorber, reabsorber, drying tower, dethanizer, Acetylene converter, ethylene rectifying column that the saturated hydrocarbons, which cracks gas separating system,；Wherein, pyrolysis furnace connects absorption tower after being sequentially connected waste heat boiler, quenching water column, compressor, and absorption tower tower top is connect with reabsorber, and tower reactor is connect with desorber；It connect after desorption column overhead connection drying tower with dethanizer, is connect at the top of tower reactor and absorption tower；Deethanizer overhead is sequentially connected with Acetylene converter, ethylene rectifying column；Ethylene distillation column overhead is connect with compressor, and tower reactor is connect with pyrolysis furnace, and side is connected with polymer grade ethylene product extraction line.Apparatus and method of the present invention is with low investment, and low energy consumption, simple process, and rate of return on investment is high.
Description
Technical Field
The invention belongs to the field of refinery saturated resource utilization, and particularly relates to a saturated hydrocarbon cracking gas separation system and an ethane/propane-rich saturated hydrocarbon utilization method.
Background
Ethylene and propylene are important basic chemical raw materials, and in industrial production processes, ethylene and propylene are mainly produced through a steam cracking (i.e., thermal cracking) process. In a steam cracking production device, cracking raw materials such as light hydrocarbon, naphtha, hydrogenation tail oil, light diesel oil and the like are mixed with steam and then subjected to thermal cracking reaction in a cracking furnace to generate cracking products such as hydrogen, methane, carbon two, carbon three, carbon four, carbon five, cracking gasoline, cracking fuel oil, coke and the like. Separating and purifying the cracking product in a subsequent separation system to obtain fractions with different carbon atoms, and separating ethylene and propylene products from the carbon two and carbon three fractions.
At present, the separation and purification of the cracking products in the industry mainly adopts a sequential separation method, a front depropanization process, a front deethanization process and the like, and the obtained products comprise polymer-grade ethylene, polymer-grade propylene and the like. However, no matter what separation process is adopted, if a rectification method is adopted to separate out light components such as methane, a cold box is required to provide lower cold energy, the investment is large, and the energy consumption is high.
A large amount of tail gas is generated in the oil refining and chemical production processes, wherein some tail gas, such as tail gas generated in the production processes of catalytic cracking, thermal cracking, delayed coking, hydrocracking and the like, contains a plurality of components of carbon and carbon, and particularly, the ethane content in some tail gas is higher. At present, carbon two and three concentrated gases recovered from refinery tail gas are mainly sent to different sections of an ethylene plant to increase the yield of ethylene and propylene, however, for a refinery without an ethylene production device at the periphery, the direction of the concentrated gases is a main problem, so that carbon two and three resources in dry gases cannot be fully utilized, and great waste is caused. If the traditional cracking compression cryogenic separation method is adopted to treat saturated resources and ethane and propane in dry gas, the investment recovery rate is low, and the energy consumption is high.
Therefore, there is a need to develop a new method and apparatus for utilizing carbon two and three saturated resources.
Disclosure of Invention
The invention aims to provide a saturated hydrocarbon cracking gas separation system and an ethane/propane-rich saturated hydrocarbon utilization method aiming at the problem of utilization of saturated dry gas resources without a matched ethylene production device, and the system has the characteristics of low investment, low energy consumption, simple process, high investment recovery rate and the like.
A first aspect of the present invention provides a saturated hydrocarbon pyrolysis gas separation system, including: the system comprises a cracking furnace, a waste heat boiler, a quenching water tower, a compressor, an absorption tower, a desorption tower, a reabsorption tower, a drying tower, a deethanization tower, a carbon dioxide hydrogenation reactor and an ethylene rectifying tower; wherein,
the cracking furnace is connected with the waste heat boiler, the quenching water tower and the compressor in sequence and then connected with the absorption tower, the top of the absorption tower is connected with the reabsorption tower, and the tower kettle is connected with the desorption tower; the top of the desorption tower is connected with the drying tower and then connected with the deethanizer, and the tower kettle is connected with the top of the absorption tower; the top of the deethanizer is connected with a carbo-hydrogenation reactor and an ethylene rectifying tower in sequence; the top of the ethylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part is connected with a polymer grade ethylene product extraction line.
According to a preferred embodiment of the present invention, the saturated hydrocarbon pyrolysis gas separation system further includes: a depropanizing tower, a carbon-three hydrogenation reactor and a propylene rectifying tower;
the tower kettle of the deethanizer is connected with the depropanizer, the tower top of the depropanizer is sequentially connected with the C-III hydrogenation reactor and the propylene rectifying tower, and the tower kettle is connected with a liquefied gas product extraction line; the top of the propylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part is connected with a polymer-grade propylene product extraction line.
When the propylene treatment device is not arranged, the tower bottom of the deethanizer is connected with a liquefied gas product extraction pipeline, and the tower bottom material is extracted as a liquefied gas product.
According to the invention, the liquid phase in the tower bottom of the reabsorption tower can be directly extracted as a product and sent to the outside of a boundary area, and a gasoline stabilizing tower can also be arranged to recover the reabsorber. Preferably, the saturated hydrocarbon cracking gas separation system further comprises a gasoline stabilizer, a tower kettle of the reabsorption tower is connected with the gasoline stabilizer, the tower top of the gasoline stabilizer is connected with the tower top of the absorption tower and/or is connected with a liquefied gas product extraction line, and the tower kettle is connected with the top of the reabsorption tower. The present invention is not particularly limited to a gasoline stabilizer, and those skilled in the art can arrange it in a conventional manner according to the prior art.
According to the present invention, preferably, the saturated hydrocarbon pyrolysis gas separation system further includes:
the quenching oil tower is used for cooling pretreatment of the discharge of the cracking furnace; and/or
A stripper column for stripping light components from the compressor interstage cooled hydrocarbons.
In the step of temperature reduction pretreatment, the invention can be provided with a quenching oil tower or not, and the temperature reduction pretreatment can be determined according to the composition of pyrolysis gas generated by different materials entering the pyrolysis furnace. The quench oil tower of the present invention is not particularly limited and can be configured in a conventional manner according to the prior art by those skilled in the art.
According to the invention, when hydrocarbons are cooled down between the compression sections, light components such as carbon, carbon and the like can be stripped out through the stripping tower and returned to the inlet of the compressor, and other components are extracted as products. The stripping column is not particularly restricted by the present invention and can be arranged by a person skilled in the art in a conventional manner according to the prior art.
In the invention, the tower kettle of the absorption tower and/or the tower kettle of the desorption tower are/is preferably provided with a reboiler to ensure that light components such as methane, hydrogen and the like in the tower kettle of the absorption tower are reduced below the set requirement. Wherein, the heating medium of the reboiler at the tower bottom of the absorption tower and the reboiler at the tower bottom of the desorption tower can adopt low-pressure steam or hot oil, preferably hot oil, which can not only fully utilize the abundant heat of a refinery, but also reduce the process energy consumption.
According to the invention, part of the absorbent enters the reabsorption tower along with the gas phase at the top of the main absorption tower, therefore, a stream of absorbent is preferably introduced into the bottom of the desorption tower to be used as supplement so as to ensure the dosage of the absorbent in the main absorption tower in the system, and similarly, a stream of reabsorber is also preferably introduced into the reabsorption tower to be used as supplement. Therefore, preferably, the absorption column is provided with an absorbent make-up line and/or the reabsorber column is provided with a reabsorber make-up line.
Fig. 2 shows a preferred embodiment of the present invention of a saturated hydrocarbon cracked gas separation system, which comprises: cracking furnace, waste heat boiler, quench water tower, compressor, absorption tower, desorption tower, reabsorption tower, gasoline stabilizer, drying tower, deethanization tower, carbon two hydrogenation reactor, ethylene rectifying tower, depropanization tower, carbon three hydrogenation reactor, propylene rectifying tower; wherein,
the cracking furnace is connected with the waste heat boiler, the quench water tower and the compressor in sequence and then connected with the middle part of the absorption tower, the top of the absorption tower is connected with the reabsorption tower, and the tower kettle is connected with the desorption tower; the tower kettle of the reabsorption tower is connected with the gasoline stabilizing tower, the tower top of the gasoline stabilizing tower is connected with a liquefied gas product extraction line, and the tower kettle is connected with the top of the reabsorption tower; the top of the desorption tower is connected with the drying tower and then connected with the middle part of the deethanizer, and the tower kettle is connected with the top of the absorption tower; the top of the deethanizer is connected with a carbon hydrogenation reactor and the middle part of an ethylene rectifying tower in sequence; the top of the ethylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part of the tower kettle is connected with a polymerization-grade ethylene product extraction line; the tower kettle of the deethanizer is connected with the middle part of the depropanizer, the tower top of the depropanizer is sequentially connected with the C-III hydrogenation reactor and the middle part of the propylene rectifying tower, and the tower kettle is connected with a liquefied gas product extraction line; the top of the propylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part of the tower kettle is connected with a polymer-grade propylene product extraction line; the absorption tower is provided with a supplemental absorbent line and the reabsorption tower is provided with a supplemental reabsorber line.
In a second aspect, the present invention provides a method for utilizing ethane/propane-rich saturated hydrocarbons, the method comprising: the ethane/propane-rich saturated hydrocarbon firstly enters a cracking furnace for cracking, then enters a compressor for boosting after being cooled by a waste heat boiler and a quench water tower, then enters an absorption tower for removing light components and enters a desorption tower, carbon-two carbon-three concentrated gas is extracted from the top of the desorption tower, and enters a deethanizer after being dried, the material at the top of the deethanizer firstly enters an ethylene rectifying tower after acetylene hydrocarbon is removed by a carbon-two hydrogenation reactor, the material at the top of the ethylene rectifying tower returns to the compressor section, the material at the bottom of the tower returns to the cracking furnace, and a polymerization-grade ethylene product is extracted at the side line.
In the present invention, the "ethane/propane-rich saturated hydrocarbon" includes both ethane-rich saturated hydrocarbon and propane-rich saturated hydrocarbon, and also includes a mixture of both, specifically including but not limited to: tail gas generated in the production processes of catalytic cracking, thermal cracking, delayed coking and hydrocracking.
In the present invention, the light components include methane and hydrogen.
According to the invention, preferably, the tower bottom material of the deethanizer enters a depropanizer, the top material of the depropanizer firstly passes through a carbon-three hydrogenation reactor to remove alkyne dialkene and then enters a propylene rectifying tower, the top material of the propylene rectifying tower returns to a compressor section, the tower bottom material returns to a cracking furnace, and a polymerization-grade propylene product is collected at the side line.
According to a preferred embodiment of the invention, the method comprises the steps of:
(1) cracking: introducing the ethane/propane-rich saturated hydrocarbon into a cracking furnace, and cracking to obtain a mixture rich in ethylene and propylene components;
(2) cooling pretreatment: the mixture rich in ethylene and propylene enters a waste heat boiler to recover heat, and then is cooled by a quenching water tower;
(3) compression: after the pressure of cracked gas coming out of the quenching water tower is increased and cooled, the cracked gas enters an absorption tower;
(4) absorption: the absorbent enters the absorption tower from the top of the absorption tower to absorb the components of C2 and above in the cracked gas; the tower bottom material flow of the absorption tower is sent to a desorption tower, and the gas material flow which is not absorbed at the tower top enters a reabsorption tower;
(5) and (3) resorption: the reabsorber enters from the top of the reabsorber to absorb the carried-out absorbent and unabsorbed C2 components, and fuel gas is produced at the top of the reabsorber;
(6) desorbing: the top of the desorption tower obtains carbon dioxide three concentrated gas, the bottom of the desorption tower obtains a poor solvent, and the poor solvent returns to the top of the absorption tower after being cooled;
(7) deethanizing: drying the concentrated carbon-two carbon-three gas obtained from the top of the desorption tower, sending the dried concentrated carbon-two carbon-three gas to a deethanizer, sending the crude ethylene gas obtained from the top of the deethanizer to a carbon-two hydrogenation reactor, taking more than three carbon components in the deethanizer as a liquefied gas product, and sending the liquefied gas product or sending the liquefied gas product to a depropanizer;
(8) refining ethylene: removing alkyne in the crude ethylene gas in a carbon-dioxide hydrogenation reactor, cooling, sending to an ethylene rectifying tower, extracting a polymerization-grade ethylene product from the side line of the ethylene rectifying tower, returning the gas phase at the top of the tower to the space between compressor sections, and returning ethane to a cracking furnace;
when the deethanizer bottoms are sent to the depropanizer, the process further comprises:
(9) depropanizing: the materials in the kettle of the deethanizer are sent to a depropanizer, a crude propylene stream is obtained at the top of the tower and sent to a carbon-three hydrogenation reactor, and the kettle of the tower contains more than four carbon components and is extracted as a liquefied gas product;
(10) and (3) propylene refining: and the crude propylene stream enters a carbon-three hydrogenation reactor to remove alkyne and diene, then enters a propylene rectifying tower, a polymerization-grade propylene product is extracted from the side line, the gas phase at the top of the tower returns to the space between the compressor sections, and propane is in the tower kettle and returns to the cracking furnace.
According to the invention, preferably, the tower bottom liquid of the reabsorption tower enters the gasoline stabilizer, the material flow at the top of the gasoline stabilizer can be returned to the top of the absorption tower for recycling, and can also be taken as liquefied gas product for extraction, and the lean reabsorber extracted from the tower bottom returns to the top of the reabsorption tower after cooling. The specific arrangement of the gasoline stabilizer is not particularly limited, and the arrangement can be set according to the conventional mode in the field, preferably, the number of theoretical plates of the gasoline stabilizer is 20-40, and the operating pressure is 0.2-1.0 MPa.
In the compression step, the number of stages to be compressed is not particularly limited in the present invention, and five-stage compression is preferably employed. Preferably, the step of boosting and cooling comprises: compressing to increase the pressure of the cracking gas to 3-5 MPag, and then cooling to 10-15 ℃; the required cold energy can be provided by a propylene refrigeration compressor or a lithium bromide refrigeration unit.
In the absorption step, the amount of the absorbent used in the absorption column is not particularly limited in the present invention, and can be determined by those skilled in the art based on the general knowledge of the prior art. The absorbent can be a carbon three-fraction containing propane, a carbon four-fraction containing n-butane and isobutane, or a carbon five-fraction containing n-pentane and isopentane; the carbon four-cut fraction containing n-butane and isobutane is preferred.
Preferably, the number of theoretical plates of the absorption tower is 25-60, the operating pressure is 2.0-6.0 MPa, and the tower top temperature is 10-40 ℃.
In the reabsorption step, the reabsorber may be gasoline, heavy naphtha or aromatic raffinate, preferably a stable gasoline component of a refinery.
Preferably, the number of theoretical plates of the reabsorption tower is 15-50, the operating pressure is 2.0-6.0 MPa, and the tower top temperature is 10-40 ℃.
In the desorption step, the desorbed absorbent obtained at the bottom of the desorption tower can be cooled step by step and then returned to the absorption tower for recycling.
According to the invention, the number of theoretical plates of the desorption tower is preferably 20-60, and the operating pressure is preferably 1.0-4.0 MPa.
According to the present invention, the present invention does not particularly limit the specific method of drying in the deethanizing step, and those skilled in the art can select various drying methods in the prior art.
According to the invention, the number of theoretical plates of the deethanizer is preferably 25-80, and the operating pressure is preferably 1.5-6.0 MPa.
In the ethylene refining step, the present invention does not specifically limit the form of the hydrogenation reactor and the catalyst, and those skilled in the art can determine the form based on the general knowledge of the prior art.
According to the invention, the number of theoretical plates of the ethylene rectifying tower is preferably 50-120, and the operating pressure is preferably 1.0-4.0 MPa.
In the depropanization step, preferably, the theoretical plate number of the depropanization tower is 25-80, and the operating pressure is 0.1-4.0 MPa.
In the propylene purification step, the form of the hydrogenation reactor and the catalyst are not particularly limited in the present invention, and those skilled in the art can determine the form based on the general knowledge of the prior art.
According to the invention, the number of theoretical plates of the propylene rectifying tower is preferably 80-280, and the operating pressure is preferably 0.1-4.0 MPa.
In the present invention, all the pressures are gauge pressures unless otherwise specified.
The method of the invention can also comprise a step of removing acid gas, wherein the acid gas removing treatment is carried out before the absorption tower or after the gas phase is extracted from the top of the desorption tower, the acid gas can be removed by amine washing or alkali washing, the acid gas is preferably removed after the desorption, and the acid gas is preferably removed by alkali washing. Acid gas is removed after desorption, so that the amount of the acid gas entering the alkaline washing/amine washing tower is greatly reduced, and the energy consumption is saved.
The method for utilizing the ethane/propane-rich saturated hydrocarbon has the following characteristics:
(1) because the absorption-desorption method is adopted to remove light components such as methane, hydrogen and the like, a complete set of equipment such as a cold box and an ethylene refrigeration compressor is not needed, the energy consumption is saved, and the investment is obviously reduced.
(2) The products are polymer-grade ethylene and polymer-grade propylene, the product quality is high, and the economic benefit is obvious.
(3) The absorbent has good selectivity, and each absorbent has ideal absorption effect, and the most suitable absorbent can be selected according to the conditions of different manufacturers.
(4) The invention provides a saturated resource utilization method with low investment, low energy consumption and obvious benefit for enterprises which have certain saturated resources but no ethylene production devices around the enterprises.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
Exemplary embodiments of the present invention will be described in more detail by referring to the accompanying drawings.
Fig. 1 is a schematic diagram of a saturated hydrocarbon pyrolysis gas separation system according to an embodiment of the present invention.
Fig. 2 is a schematic diagram of a saturated hydrocarbon cracked gas separation system according to another embodiment of the present invention.
Description of reference numerals:
1, a cracking furnace; 2 a waste heat boiler; 3, a quench water tower; 4, a compressor; 5 an absorption tower; 6 a desorption tower; 7 a reabsorption column; 8, a gasoline stabilizer; 9, a drying tower; 10 a deethanizer; 11 an ethylene rectification column; 12 a hydrogenation reactor for carbon dioxide; 13 a depropanizer; 14, a propylene rectifying tower; 15-carbon three-hydrogenation reactor; 16 saturated resources; 17 a fuel gas; 18 make-up reabsorber; 19 supplementing the absorbent; 20 polymer grade ethylene product; 21 polymer grade propylene product; 22 liquefied gas product.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below.
The present invention will be further described with reference to the following examples.
Example 1:
a saturated hydrocarbon cracking gas separation system shown in figure 1 is adopted, which comprises: the system comprises a cracking furnace 1, a waste heat boiler 2, a quench water tower 3, a compressor 4, an absorption tower 5, a desorption tower 6, a reabsorption tower 7, a gasoline stabilizing tower 8, a drying tower 9, a deethanizer 10, an ethylene rectifying tower 11 and a carbon dioxide hydrogenation reactor 12.
The cracking furnace 1 is connected with a waste heat boiler 2, a quench water tower 3 and a compressor 4 in sequence and then connected with the middle part of an absorption tower 5, the top of the absorption tower 5 is connected with a reabsorption tower 7, and the tower kettle is connected with a desorption tower 6; the bottom of the reabsorption tower 7 is connected with a gasoline stabilizer 8, the top of the gasoline stabilizer 8 is connected with a liquefied gas product extraction line, and the bottom of the tower is connected with the top of the reabsorption tower 7; the top of the desorption tower 6 is connected with a drying tower 9 and then is connected with the middle part of a deethanizer 10, and the tower kettle is connected with the top of the absorption tower 5; the top of the deethanizer 10 is connected with a carbo-hydrogenation reactor 12 and the middle part of an ethylene rectifying tower 11 in sequence; the top of the ethylene rectifying tower 11 is connected with a compressor 4, the tower kettle is connected with a cracking furnace 1, and the side part is connected with a polymer-grade ethylene product extraction line; the tower kettle of the deethanizer 10 is connected with a liquefied gas product extraction line; the absorption tower 5 is provided with a supplemental absorbent line and the reabsorption tower 7 is provided with a supplemental reabsorber line.
The saturated resource is ethane, and the amount of ethane entering the cracking furnace is 37500 kg/h. N-butane is selected as an absorbent, and gasoline is selected as a reabsorber.
The utilization method of the ethane/propane-rich saturated hydrocarbon comprises the following steps:
(1) cracking: ethane is firstly cracked in the cracking furnace 1 to obtain ethane cracked gas.
(2) Cooling pretreatment: ethane cracked gas enters a waste heat boiler 2 to recover heat, and is cooled by a quenching water tower 3.
(3) Compression: the ethane cracked gas from the quenching water tower 3 is compressed for five sections to increase the cracked gas pressure to 4MPag, then cooled to 15 ℃, and enters an absorption tower 5.
(4) Absorption: the theoretical plate number of the absorption column 5 was 40, the operating pressure was 3.8MPag, and the column top temperature was 15 ℃. The absorption solvent is saturated carbon four, the solvent enters the absorption tower from the top of the absorption tower 5, and the dry gas enters from the 15 th tower plate. C2 and its heavy components in the dry gas are absorbed by solvent and extracted from tower bottom, and the tower top contains light components of methane, hydrogen, etc. and a small amount of absorbent.
(5) Desorbing: the theoretical plate number of the desorber 6 was 40 and the operating pressure was 2.2 MPag. The rich solvent absorbing the components such as C2 in the dry gas enters a desorption tower from the 20 th tower plate, the desorbed C2 concentrated gas is extracted from the top of the tower, and the lean solvent is cooled to 15 ℃ after being subjected to gradual heat exchange and returns to the absorption tower 5 for recycling.
(6) A resorption system: the gas not absorbed at the top of the absorption column was introduced into a reabsorption column 7, the theoretical plate number of the reabsorption column 7 was 20, the operation pressure was 3.5MPag, and the temperature at the top of the column was 15 ℃. The reabsorbing agent adopts stable gasoline, enters the reabsorbing tower 7 from the top of the tower, and absorbs the carbon two component and the carbon four absorbent. The tower bottom of the reabsorption tower 7 is rich gasoline, and after the rich gasoline is sent to the gasoline stabilizer 8 for desorption, the poor reabsorber returns to the reabsorber 7 for recycling. Components such as methane and hydrogen are extracted from the top of the reabsorption tower and are directly discharged into a fuel gas pipe network, and the material flow at the top of the gasoline stabilizer 8 is extracted as a liquefied gas product. The theoretical plate number of the gasoline stabilizer 8 was 28 and the operating pressure was 0.5 MPag.
(7) Deethanizing: the carbon dioxide three-concentrated gas obtained from the top of the desorption tower 6 is dried and then sent to the deethanizer 10, the number of theoretical plates of the deethanizer 10 is 50, and the operating pressure is 1.9 MPag. Crude ethylene gas is extracted from the tower top and sent to a carbon dioxide hydrogenation reactor 12, and the tower bottom contains more than three carbon components and is extracted as a liquefied gas product 22.
(8) Refining ethylene: the crude ethylene gas is removed by acetylene and other alkyne reaction in a carbon hydrogenation reactor 12, and then is sent to an ethylene rectifying tower 11 after being cooled, the theoretical plate number of the ethylene rectifying tower 11 is 90, and the operating pressure is 1.8 MPag. The polymerization-grade ethylene product 20 is extracted from the side line of the ethylene rectifying tower 11, the gas phase at the top of the tower returns to the second-section inlet of the compressor 4, and the ethane at the bottom of the tower returns to the cracking furnace 1.
The composition of the ethane cracked gas after passing through the quench water tower is shown in table 2.
TABLE 2 cracked gas composition
| Composition of | mol％ |
| Hydrogen gas | 35.30 |
| Methane | 3.36 |
| Acetylene | 0.24 |
| Ethylene | 32.71 |
| Ethane (III) | 20.56 |
| Allene | 0.02 |
| Propylene (PA) | 0.02 |
| Propylene (PA) | 0.34 |
| Propane | 0.06 |
| Butadiene | 0.37 |
| Butene (butylene) | 0.06 |
| Butane | 0.06 |
| C5+ | 0.38 |
| Water (W) | 6.53 |
The composition of the polymer grade ethylene product obtained is shown in table 3.
TABLE 3 Polymer grade ethylene product composition
| Composition of | mol％ |
| Methane | 0.02 |
| Ethylene | 99.98 |
In this example, the ethylene recovery was 99.6%.
Example 2:
a saturated hydrocarbon cracking gas separation system shown in figure 2 is adopted, which comprises: the system comprises a cracking furnace 1, a waste heat boiler 2, a quench water tower 3, a compressor 4, an absorption tower 5, a desorption tower 6, a reabsorption tower 7, a gasoline stabilizing tower 8, a drying tower 9, a deethanizer 10, an ethylene rectifying tower 11, a carbon dioxide hydrogenation reactor 12, a depropanizer 13, a propylene rectifying tower 14 and a carbon three hydrogenation reactor 15.
The cracking furnace 1 is connected with a waste heat boiler 2, a quench water tower 3 and a compressor 4 in sequence and then connected with the middle part of an absorption tower 5, the top of the absorption tower 5 is connected with a reabsorption tower 7, and the tower kettle is connected with a desorption tower 6; the bottom of the reabsorption tower 7 is connected with a gasoline stabilizer 8, the top of the gasoline stabilizer 8 is connected with a liquefied gas product extraction line, and the bottom of the tower is connected with the top of the reabsorption tower 7; the top of the desorption tower 6 is connected with a drying tower 9 and then is connected with the middle part of a deethanizer 10, and the tower kettle is connected with the top of the absorption tower 5; the top of the deethanizer 10 is connected with a carbo-hydrogenation reactor 12 and the middle part of an ethylene rectifying tower 11 in sequence; the top of the ethylene rectifying tower 11 is connected with a compressor 4, the tower kettle is connected with a cracking furnace 1, and the side part is connected with a polymer-grade ethylene product extraction line; the bottom of the deethanizer 10 is connected with the middle of the depropanizer 13, the top of the depropanizer 13 is connected with the C-III hydrogenation reactor 15 and the middle of the propylene rectifying tower 14 in sequence, and the bottom of the tower is connected with a liquefied gas product extraction line; the top of the propylene rectifying tower 14 is connected with a compressor 4, the tower kettle is connected with the cracking furnace 1, and the side part is connected with a polymer-grade propylene product extraction line; the absorption tower 5 is provided with a supplemental absorbent line and the reabsorption tower 7 is provided with a supplemental reabsorber line.
The saturated resources are ethane and propane, the ethane feed into the cracking furnace is 20000kg/h, and the propane feed into the cracking furnace is 17500 kg/h. N-butane is selected as an absorbent, and gasoline is selected as a reabsorber.
The method for utilizing the ethane/propane-rich saturated hydrocarbon comprises the steps (1) to (8) which are the same as the step 1, except that the material in the deethanizer in the step (7) is sent to a depropanizer 13;
the method further comprises the following steps:
(9) depropanizing: the materials in the bottom of the deethanizer are sent to a depropanizer 13, the theoretical plate number of the depropanizer 13 is 40, and the operation pressure is 0.7 Mpag. Crude propylene material flow is obtained at the top of the depropanizing tower 13 and sent to a carbon three hydrogenation reactor 15, and the tower bottom contains more than four carbon components and is taken out as a liquefied gas product 22.
(10) And (3) propylene refining: the crude propylene stream enters a carbon hydrogenation reactor 15, acetylene hydrocarbon and diene in the crude propylene stream are removed through reaction, and then the crude propylene stream enters a propylene rectifying tower 14, the number of theoretical plates of the propylene rectifying tower 14 is 170, and the operating pressure is 1.7 MPag. The polymerization-grade propylene product 21 is extracted from the side line of the propylene rectifying tower 14, the gas phase at the top of the tower returns to the two-section suction tank of the compressor 4, and the propane at the bottom of the tower returns to the cracking furnace 1.
The composition of the cracked gas after passing through the quench water tower is shown in Table 4.
TABLE 4 cracked gas composition after quench water tower
| Composition of | mol％ |
| Hydrogen gas | 26.52 |
| Methane | 15.41 |
| Acetylene | 0.30 |
| Ethylene | 31.20 |
| Ethane (III) | 13.19 |
| Allene | 0.05 |
| Propyne | 0.07 |
| Propylene (PA) | 3.08 |
| Propane | 1.64 |
| Butadiene | 0.83 |
| Butene (butylene) | 0.18 |
| Butane | 0.05 |
| C5+ | 0.96 |
| Water (W) | 6.53 |
The resulting polymer grade ethylene product and polymer grade propylene product compositions are shown in tables 5 and 6.
TABLE 5 Polymer grade ethylene product compositions
| Composition of | mol％ |
| Methane | 0.02 |
| Ethylene | 99.98 |
TABLE 6 Polymer grade propylene product composition
| Composition of | mol％ |
| Ethylene | 0.008 |
| Ethane (III) | 0.04 |
| Propylene (PA) | 99.7 |
| Propane | 0.252 |
In this example, the ethylene recovery was 99.5% and the propylene recovery was 98%.
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 (13)
1. A saturated hydrocarbon pyrolysis gas separation system is characterized by comprising: the system comprises a cracking furnace, a waste heat boiler, a quenching water tower, a compressor, an absorption tower, a desorption tower, a reabsorption tower, a drying tower, a deethanization tower, a carbon dioxide hydrogenation reactor and an ethylene rectifying tower; wherein,
the cracking furnace is connected with the waste heat boiler, the quenching water tower and the compressor in sequence and then connected with the absorption tower, the top of the absorption tower is connected with the reabsorption tower, and the tower kettle is connected with the desorption tower; the top of the desorption tower is connected with the drying tower and then connected with the deethanizer, and the tower kettle is connected with the top of the absorption tower; the top of the deethanizer is connected with a carbo-hydrogenation reactor and an ethylene rectifying tower in sequence; the top of the ethylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part is connected with a polymer grade ethylene product extraction line.
2. The saturated hydrocarbon cracked gas separation system of claim 1, wherein the saturated hydrocarbon cracked gas separation system further comprises: a depropanizing tower, a carbon-three hydrogenation reactor and a propylene rectifying tower;
the tower kettle of the deethanizer is connected with the depropanizer, the tower top of the depropanizer is sequentially connected with the C-III hydrogenation reactor and the propylene rectifying tower, and the tower kettle is connected with a liquefied gas product extraction line; the top of the propylene rectifying tower is connected with a compressor, the tower kettle is connected with a cracking furnace, and the side part is connected with a polymer-grade propylene product extraction line.
3. The saturated hydrocarbon cracking gas separation system of claim 1, further comprising a gasoline stabilizer, wherein a tower kettle of the reabsorption tower is connected with the gasoline stabilizer, the tower top of the gasoline stabilizer is connected with the tower top of the absorption tower and/or is connected with a liquefied gas product extraction line, and the tower kettle is connected with the top of the reabsorption tower.
4. The saturated hydrocarbon cracked gas separation system of claim 1, wherein the saturated hydrocarbon cracked gas separation system further comprises:
the quenching oil tower is used for cooling pretreatment of the discharge of the cracking furnace; and/or
A stripper column for stripping light components from the compressor interstage cooled hydrocarbons.
5. The saturated hydrocarbon pyrolysis gas separation system according to claim 1, wherein the absorption column bottom and/or the desorption column bottom is provided with a reboiler.
6. The saturated hydrocarbon cracked gas separation system as claimed in any one of claims 1 to 5, wherein,
the absorption tower is provided with an absorbent make-up line, and/or
The reabsorber column is provided with a reabsorber replenishment line.
7. A process for utilizing ethane/propane rich saturated hydrocarbons, the process comprising: the ethane/propane-rich saturated hydrocarbon firstly enters a cracking furnace for cracking, then enters a compressor for boosting after being cooled by a waste heat boiler and a quench water tower, then enters an absorption tower for removing light components and enters a desorption tower, carbon-two carbon-three concentrated gas is extracted from the top of the desorption tower, and enters a deethanizer after being dried, the material at the top of the deethanizer firstly enters an ethylene rectifying tower after acetylene hydrocarbon is removed by a carbon-two hydrogenation reactor, the material at the top of the ethylene rectifying tower returns to the compressor section, the material at the bottom of the tower returns to the cracking furnace, and a polymerization-grade ethylene product is extracted at the side line.
8. The method for utilizing ethane/propane-rich saturated hydrocarbons according to claim 7, wherein the material at the bottom of the deethanizer enters a depropanizer, the material at the top of the depropanizer enters a propylene rectifying tower after acetylene hydrocarbon diene is removed from the material by a carbon-three hydrogenation reactor, the material at the top of the propylene rectifying tower returns to the space between compressor sections, the material at the bottom of the tower returns to the cracking furnace, and the polymerization-grade propylene product is collected at the side line.
9. The method of utilizing ethane/propane-rich saturated hydrocarbons according to claim 7, wherein the method comprises the steps of:
(1) cracking: introducing the ethane/propane-rich saturated hydrocarbon into a cracking furnace, and cracking to obtain a mixture rich in ethylene and propylene components;
(2) cooling pretreatment: the mixture rich in ethylene and propylene enters a waste heat boiler to recover heat, and then is cooled by a quenching water tower;
(3) compression: after the pressure of cracked gas coming out of the quenching water tower is increased and cooled, the cracked gas enters an absorption tower;
(4) absorption: the absorbent enters the absorption tower from the top of the absorption tower to absorb the components of C2 and above in the cracked gas; the tower bottom material flow of the absorption tower is sent to a desorption tower, and the gas material flow which is not absorbed at the tower top enters a reabsorption tower;
(5) and (3) resorption: the reabsorber enters from the top of the reabsorber to absorb the carried-out absorbent and unabsorbed C2 components, and fuel gas is produced at the top of the reabsorber;
(6) desorbing: the top of the desorption tower obtains carbon dioxide three concentrated gas, the bottom of the desorption tower obtains a poor solvent, and the poor solvent returns to the top of the absorption tower after being cooled;
(7) deethanizing: drying the concentrated carbon-two carbon-three gas obtained from the top of the desorption tower, sending the dried concentrated carbon-two carbon-three gas to a deethanizer, sending the crude ethylene gas obtained from the top of the deethanizer to a carbon-two hydrogenation reactor, taking more than three carbon components in the deethanizer as a liquefied gas product, and sending the liquefied gas product or sending the liquefied gas product to a depropanizer;
(8) refining ethylene: removing alkyne in the crude ethylene gas in a carbon-dioxide hydrogenation reactor, cooling, sending to an ethylene rectifying tower, extracting a polymerization-grade ethylene product from the side line of the ethylene rectifying tower, returning the gas phase at the top of the tower to the space between compressor sections, and returning ethane to a cracking furnace;
when the deethanizer bottoms are sent to the depropanizer, the process further comprises:
(9) depropanizing: the materials in the kettle of the deethanizer are sent to a depropanizer, a crude propylene stream is obtained at the top of the tower and sent to a carbon-three hydrogenation reactor, and the kettle of the tower contains more than four carbon components and is extracted as a liquefied gas product;
(10) and (3) propylene refining: and the crude propylene stream enters a carbon-three hydrogenation reactor to remove alkyne and diene, then enters a propylene rectifying tower, a polymerization-grade propylene product is extracted from the side line, the gas phase at the top of the tower returns to the space between the compressor sections, and propane is in the tower kettle and returns to the cracking furnace.
10. The utilization method of the ethane/propane-rich saturated hydrocarbon according to claim 7, wherein the bottom liquid of the reabsorption tower enters a gasoline stabilizer, the material flow at the top of the gasoline stabilizer returns to the top of the absorption tower for recycling and/or is extracted as a liquefied gas product, the lean reabsorber is extracted from the bottom of the tower and returns to the top of the reabsorber after being cooled;
the number of theoretical plates of the gasoline stabilizer is 20-40, and the operating pressure is 0.2-1.0 MPa.
11. The method of utilizing an ethane/propane-rich saturated hydrocarbon according to any one of claims 7 to 10,
the number of theoretical plates of the absorption tower is 25-60, the operating pressure is 2.0-6.0 MPa, and the temperature at the top of the tower is 10-40 ℃; the absorbent is a carbon three-fraction containing propane, a carbon four-fraction containing n-butane and isobutane, or a carbon five-fraction containing n-pentane and isopentane;
the number of theoretical plates of the reabsorption tower is 15-50, the operating pressure is 2.0-6.0 MPa, and the temperature of the tower top is 10-40 ℃; the reabsorber is gasoline, heavy naphtha or aromatic raffinate oil.
12. The method for utilizing an ethane/propane-rich saturated hydrocarbon according to any one of claims 7 to 10, wherein the method further comprises an acid gas removal step of performing acid gas removal treatment before entering the absorption tower or after withdrawing a gas phase from the top of the desorption tower.
13. The method of utilizing an ethane/propane-rich saturated hydrocarbon according to any one of claims 7 to 10,
the step of boosting and cooling comprises: compressing to increase the pressure of the cracking gas to 3-5 MPag, and then cooling to 10-15 ℃;
the number of theoretical plates of the desorption tower is 20-60, and the operating pressure is 1.0-4.0 MPa;
the number of theoretical plates of the deethanizer is 25-80, and the operating pressure is 1.5-6.0 MPa;
the number of theoretical plates of the ethylene rectifying tower is 50-120, and the operating pressure is 1.0-4.0 MPa;
the number of theoretical plates of the depropanizing tower is 25-80, and the operating pressure is 0.1-4.0 MPa;
the number of theoretical plates of the propylene rectifying tower is 80-280, and the operating pressure is 0.1-4.0 MPa.
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