CN105026342A - Ethylene production apparatus and method - Google Patents
Ethylene production apparatus and method Download PDFInfo
- Publication number
- CN105026342A CN105026342A CN201480014164.8A CN201480014164A CN105026342A CN 105026342 A CN105026342 A CN 105026342A CN 201480014164 A CN201480014164 A CN 201480014164A CN 105026342 A CN105026342 A CN 105026342A
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- China
- Prior art keywords
- ethene
- concentration
- naphtha
- straight chain
- manufacturing installation
- Prior art date
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 143
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 77
- 238000000034 method Methods 0.000 title claims description 50
- 239000005977 Ethylene Substances 0.000 title abstract description 5
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 75
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 64
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 58
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 53
- 229930195734 saturated hydrocarbon Natural products 0.000 claims abstract description 53
- 239000001273 butane Substances 0.000 claims abstract description 52
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims abstract description 50
- 238000005979 thermal decomposition reaction Methods 0.000 claims abstract description 7
- -1 alkane compound Chemical class 0.000 claims description 85
- 239000003208 petroleum Substances 0.000 claims description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 77
- 238000000197 pyrolysis Methods 0.000 claims description 55
- 238000009434 installation Methods 0.000 claims description 50
- 230000008569 process Effects 0.000 claims description 37
- 238000001179 sorption measurement Methods 0.000 claims description 27
- 230000009183 running Effects 0.000 claims description 21
- 238000001149 thermolysis Methods 0.000 claims description 21
- 238000005194 fractionation Methods 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 238000009835 boiling Methods 0.000 claims description 15
- 230000007246 mechanism Effects 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 12
- 229910021536 Zeolite Inorganic materials 0.000 claims description 10
- 239000010779 crude oil Substances 0.000 claims description 10
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 10
- 239000010457 zeolite Substances 0.000 claims description 10
- 230000008520 organization Effects 0.000 claims description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 8
- 125000004122 cyclic group Chemical group 0.000 claims description 8
- 239000003345 natural gas Substances 0.000 claims description 8
- 229930195735 unsaturated hydrocarbon Natural products 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 33
- 239000006227 byproduct Substances 0.000 abstract description 11
- 150000001875 compounds Chemical class 0.000 abstract description 3
- 239000013064 chemical raw material Substances 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000001282 iso-butane Substances 0.000 abstract 1
- 239000000126 substance Substances 0.000 description 67
- 230000015572 biosynthetic process Effects 0.000 description 28
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 28
- 238000004821 distillation Methods 0.000 description 22
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical group C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 14
- 150000001335 aliphatic alkanes Chemical class 0.000 description 12
- 239000002994 raw material Substances 0.000 description 11
- 238000010586 diagram Methods 0.000 description 8
- 239000012535 impurity Substances 0.000 description 8
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 8
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000000354 decomposition reaction Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- GXDHCNNESPLIKD-UHFFFAOYSA-N 2-methylhexane Natural products CCCCC(C)C GXDHCNNESPLIKD-UHFFFAOYSA-N 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000001771 impaired effect Effects 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural parallel stages only
-
- 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
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2767—Changing the number of side-chains
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
Abstract
The concentration of linear saturated hydrocarbon compounds in the naphtha fraction is reduced and the concentration of branched saturated hydrocarbon compounds is increased by Isomerization treatment using a naphtha Isomerization (isometrization) reaction apparatus (12). The concentration of normal butane in butane is reduced and the concentration of isobutane is increased by Isomerization treatment using a butane Isomerization (isometrization) reaction apparatus (14), and thermal decomposition is performed together with steam using a steam thermal decomposition apparatus (13). The amount of production of the basic chemical raw material as a by-product with respect to the amount of production of ethylene is increased or decreased by changing the concentration of the branched saturated hydrocarbon compound with respect to the concentration of the linear saturated hydrocarbon compound to be treated with the steam thermal decomposition device (13). Both the need for ethylene and the balance of supply as well as the need for the base compound and the balance of supply can be ensured.
Description
Technical field
The present invention relates to the manufacturing installation and method thereof that manufacture ethene.
Background technology
The major part of the product of other kind manufactured in petroleum chemical plant is that raw material manufactures with ethene.This ethene is normally used for being that raw material is to manufacture the method for ethene with naphtha fraction.Like this, studying the yield (reference example as patent documentation 1,2) improving and be widely used as the ethene of raw material always.
In the manufacture method of the ethene recorded in patent documentation 1, utilize straight chain saturation alkane adsorption separation device, the naphtha fraction of raw material is separated into the high compound of straight chain saturated carbonization concentration and low compound, and using straight chain saturation alkane as ethylene raw, ethene is manufactured with water vapor pyrolysis device, make the yield of ethene improve thus, manufacture the basic chemical feedstock that the monocyclic aromatic such as propylene, divinyl, the benzene hydrocarbon of the by product manufactured as ethene etc. is important simultaneously together with ethene.
In the manufacture method of the ethene recorded in patent documentation 2, by the naphtha fraction of raw material together with the Fischer-Tropsch synthesis oil being rich in straight chain saturation alkane with water vapor pyrolysis device to manufacture ethene, make the yield of ethene improve thus, also manufacture important basic chemical feedstock simultaneously.
Prior art document
Patent documentation
Patent documentation 1: United States Patent (USP) No. 6407301 specification sheets
Patent documentation 2: Japanese Unexamined Patent Publication 6-184556 publication.
Summary of the invention
The problem that invention will solve
But even be widely used as the ethene of raw material, also there is change in its requirement, and the balance of feed rate and requirement is impaired sometimes.Now, in the situation that requirement reduces relative to feed rate, the decomposition condition of the naphtha fractions such as temperature can be adjusted, thus adjust a part of turnout, but when the balance of feed rate and requirement increases to a certain degree, then need the logical oil mass of the amount changed as process naphtha fraction, that is, the rate of capacity utilization of ethene producing apparatus.Due to the change of this rate of capacity utilization, in method in the past, turnout as the important basic chemical feedstock of the propylene or the monocyclic aromatic such as divinyl and benzene hydrocarbon etc. of the by product of the manufacture of ethene also correspondingly can change along with the turnout of ethene, thus the unfavorable condition that the balance that there is the feed rate of these basic chemical feedstock and requirement is also impaired.Namely, if realize the requirement of ethene and the balance of feed rate and reduce the rate of capacity utilization, then the turnout of the basic chemical feedstock such as propylene or the monocyclic aromatic such as divinyl and benzene hydrocarbon can reduce, and the unfavorable condition that cannot meet the needs of basic chemical feedstock occurs.
The object of this invention is to provide the growing amount that can increase the by products such as propylene relative to the manufacturing installation of the ethene of the ratio of the growing amount of ethene and method thereof.
For the method for dealing with problems
The manufacturing installation of ethene of the present invention, naphtha fraction is carried out thermolysis together with water vapor and manufactures the manufacturing installation of the ethene of ethene, it is characterized in that possessing: the petroleum naphtha treatment facility concentration of the straight chain saturation alkane compound in aforementioned naphtha fraction reduced; With the aforementioned naphtha fraction through the process of aforementioned petroleum naphtha treatment facility is carried out together with water vapor the water vapor pyrolysis device of thermolysis.
In this invention, after the concentration of straight chain saturation alkane compound being reduced with petroleum naphtha treatment facility, thermolysis is carried out together with water vapor, therefore relative to the growing amount of ethene, the ratio as the growing amount of the basic chemical feedstock such as the monocyclic aromatic such as propylene, divinyl, benzene hydrocarbon of the by product of the manufacture of ethene increases.By this, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
Then, in the present invention, be preferably following formation: aforementioned naphtha fraction is carried out isomerization process and the concentration of aforementioned linear saturated hydrocarbon compound reduced by aforementioned petroleum naphtha treatment facility, makes the concentration of branched-chain saturated hydrocarbon compound increase simultaneously.
In this invention, by carrying out isomerization process to naphtha fraction, the concentration of straight chain saturation alkane compound is reduced, make the concentration of branched-chain saturated hydrocarbon compound increase simultaneously, thus the growing amount of basic chemical feedstock can be made to increase further relative to the ratio of the growing amount of ethene, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in the present invention, following formation is preferably: aforementioned petroleum naphtha treatment facility distills aforementioned naphtha fraction and the branched-chain saturated hydrocarbon compound of separation is supplied to aforementioned water vapor pyrolysis device.
In this invention, the branched-chain saturated hydrocarbon compound of separation is also supplied to water vapor pyrolysis device by distillation naphtha fraction, thus the growing amount of basic chemical feedstock can be made to increase further relative to the ratio of the growing amount of ethene, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in the present invention, following formation is preferably: the concentration of aforementioned linear saturated hydrocarbon compound also reduces by the aforementioned linear saturated hydrocarbon compound in the aforementioned naphtha fraction of aforementioned petroleum naphtha treatment facility fractionation by adsorption.
In this invention, by the straight chain saturation alkane compound in fractionation by adsorption naphtha fraction, the concentration of straight chain saturation alkane compound is reduced, therefore easily efficiency can reduce the concentration of straight chain saturation alkane compound well.
And then, in the present invention, be preferably following formation: aforementioned petroleum naphtha treatment facility uses zeolite to carry out fractionation by adsorption aforementioned linear saturated hydrocarbon compound.
In this invention, use the straight chain saturation alkane compound that zeolite comes in fractionation by adsorption naphtha fraction, thus can easily efficiency fractionation by adsorption straight chain saturation alkane compound well, the concentration of straight chain saturation alkane compound can be reduced.Should illustrate, as zeolite, such as United States Patent (USP) No. 6407301 zeolite shown in specification sheets can be utilized aptly.
Then, in the present invention, be preferably following formation: at least wantonly 1 in cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound is mixed in aforementioned naphtha fraction by aforementioned petroleum naphtha treatment facility, the concentration of the straight chain saturation alkane compound in aforementioned naphtha fraction is reduced.
In this invention, at least wantonly 1 in cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound is mixed in naphtha fraction, thus can easily the concentration of the straight chain saturation alkane compound in naphtha fraction be reduced.
And then, in the present invention, be preferably following formation: the boiling point of aforementioned cyclic saturated hydrocarbon compound be more than 49 DEG C and less than 160 DEG C, the boiling point of aforementioned fragrance race hydrocarbon compound is more than 80 DEG C and less than 160 DEG C.
In this invention, boiling point is used to be more than 49 DEG C and less than 160 DEG C persons as cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound uses boiling point to be more than 80 DEG C and less than 160 DEG C persons, thus be same degree with the boiling point of naphtha fraction, thus directly can utilize the resolving device of former decomposition naphtha fraction.
Then, in the present invention, be preferably following formation: boiling point is more than 30 DEG C to aforementioned petroleum naphtha treatment facility and the middle runnings of less than 180 DEG C is mixed in aforementioned naphtha fraction.
In this invention, boiling point is more than 30 DEG C and the middle runnings of less than 180 DEG C is mixed in naphtha fraction, thus easily at least a kind in cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound can be mixed in naphtha fraction, the boiling point of boiling point and naphtha fraction is same degree simultaneously, directly can utilize the resolving device of decomposition naphtha fraction in the past.
In addition, in the present invention, following formation is preferably: aforementioned petroleum naphtha treatment facility reduces the concentration of aforementioned linear saturated hydrocarbon compound with the condition of the relation of following formula (1) to meet:
Concentration >=1.8 of the concentration/straight chain saturation alkane compound of branched-chain saturated hydrocarbon compound ... (1).
In this invention, by reducing the concentration of straight chain saturation alkane compound in the mode of the relation meeting above-mentioned formula (1), the growing amount of basic chemical feedstock can be made to increase further relative to the ratio of the growing amount of ethene, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
Then, in the present invention, be preferably following formation: possess and the straight chain saturation alkane compound residued in the naphtha fraction of aforementioned petroleum naphtha treatment facility process reclaimed and is returned to the foldback mechanism of aforementioned petroleum naphtha treatment facility.
In this invention, by foldback mechanism the straight chain saturation alkane compound residued in the naphtha fraction of petroleum naphtha treatment facility process reclaimed and be again returned to petroleum naphtha treatment facility and process, the concentration of the straight chain saturation alkane compound in the naphtha fraction being supplied to water vapor pyrolysis device can be reduced thus further, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
And then, in the present invention, be preferably following formation: possess the petroleum naphtha mixed organization mixing the naphtha fraction without the process of aforementioned petroleum naphtha treatment facility in the naphtha fraction through the process of aforementioned petroleum naphtha treatment facility.
In this invention, by mixing the naphtha fraction without the process of petroleum naphtha treatment facility in the naphtha fraction through the process of petroleum naphtha treatment facility, the concentration reduced of straight chain saturation alkane compound can be made to increase, the growing amount of ethene can be increased when not changing the growing amount of basic chemical feedstock, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in the present invention, following formation is preferably: possess the concentration reduction making to be refined by crude oil or natural-gas the normal butane in the butane obtained and the concentration of Trimethylmethane is increased, and be supplied to the butane treatment equipment of aforementioned water vapor pyrolysis device.
In this invention, reduce by making the concentration of being refined the normal butane of the butane obtained by crude oil or natural-gas and increase the concentration of Trimethylmethane, and be supplied to water vapor pyrolysis device, easily can reducing the concentration of the straight chain saturation alkane compound in naphtha fraction, the growing amount of ethene can be reduced when not changing the growing amount of basic chemical feedstock.
Then, in the present invention, be preferably following formation: aforementioned butane treatment equipment carries out isomerization process to aforementioned butane and the concentration of normal butane reduced, and makes the concentration of Trimethylmethane increase simultaneously.
In this invention, by carrying out isomerization process to butane, the concentration of normal butane is reduced, make the concentration of Trimethylmethane increase simultaneously, easily can increase the concentration of branched-chain saturated hydrocarbon compound, the concentration of the straight chain saturation alkane compound in the naphtha fraction with the process of water vapor pyrolysis device can be reduced and increase the concentration of branched-chain saturated hydrocarbon compound, the growing amount of ethene can be increased when not changing the growing amount of basic chemical feedstock, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
And then, in the present invention, be preferably following formation: aforementioned butane treatment equipment distills aforementioned butane, and be supplied to aforementioned water vapor pyrolysis device by being separated the Trimethylmethane obtained.
In this invention, owing to distilling butane and being supplied to water vapor pyrolysis device by being separated the Trimethylmethane obtained, thus can easily the concentration of the straight chain saturation alkane compound in the naphtha fraction with the process of water vapor pyrolysis device be reduced and increase the concentration of branched-chain saturated hydrocarbon compound.
Should illustrate that the supply to water vapor pyrolysis device of Trimethylmethane can be supplied to water vapor pyrolysis device after mixing with the petroleum naphtha processed with petroleum naphtha treatment facility, also can directly be supplied to water vapor pyrolysis device by Trimethylmethane.
The manufacture method of ethene of the present invention, naphtha fraction is carried out thermolysis together with water vapor and makes the manufacture method of the ethene of ethene, it is characterized in that, implement following step: the petroleum naphtha treatment step that the concentration of the straight chain saturation alkane compound in aforementioned naphtha fraction is reduced; With the naphtha fraction through the process of aforementioned petroleum naphtha treatment step is carried out together with water vapor the water vapor thermal decomposition steps of thermolysis.
In this invention, after the concentration of straight chain saturation alkane compound is reduced, carry out thermolysis together with water vapor, thus relative to the growing amount of ethene, the ratio as the growing amount of the basic chemical feedstock such as the monocyclic aromatic such as propylene, divinyl, benzene hydrocarbon of the by product of the manufacture of ethene increases.By this, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
Accompanying drawing explanation
[Fig. 1] illustrates the block diagram of the schematic configuration of the manufacturing installation of the ethene of the first embodiment of the present invention.
[Fig. 2] illustrates the block diagram of the schematic configuration of the manufacturing installation of the ethene of the second embodiment of the present invention.
[Fig. 3] illustrates the block diagram of the schematic configuration of the manufacturing installation of the ethene of the 3rd embodiment of the present invention.
[Fig. 4] illustrates the block diagram of the schematic configuration of the manufacturing installation of the ethene of the 4th embodiment of the present invention.
[Fig. 5] illustrates the schematic configuration diagram for illustration of experimental installation of the present invention.
Embodiment
Below, with reference to accompanying drawing, the manufacturing installation of ethene of the present invention embodiment is described.
［ the first embodiment ］
(formation of ethene manufacturing installation)
As shown in Figure 1, ethene manufacturing installation 10 makes naphtha fraction contact with water vapor and carry out thermolysis to manufacture the device of ethene.
This ethene manufacturing installation 10 possesses: impurity removal device 11, petroleum naphtha isomerization (Isomerization) conversion unit 12 as petroleum naphtha treatment facility, water vapor pyrolysis device 13, butane isomerization (Isomerization) conversion unit 14 as butane treatment equipment, foldback mechanism 15, with petroleum naphtha mixed organization 16.
Here, the naphtha fraction of raw material uses those that obtain by the refining of crude oil or natural-gas, and the concentration of use chain saturated hydrocarbon compound is more than 75 quality % and those of below 90 quality % usually.Then, the straight chain saturation alkane compound of the naphtha fraction obtained by the refining of this crude oil is roughly 1 to 1 with the ratio of branched-chain saturated hydrocarbon compound.
Impurity removal device 11 removes the impurity as catalyst poison used in petroleum naphtha isomerization (Isomerization) conversion unit 12 of back segment such as sulphur composition in naphtha fraction.
Petroleum naphtha isomerization (Isomerization) conversion unit 12 is connected to impurity removal device 11, processes the naphtha fraction processed through impurity removal device 11, reduces the concentration of the straight chain saturation alkane compound in naphtha fraction.Particularly, carry out carrying out isomerization process to naphtha fraction and reducing the concentration of straight chain saturation alkane compound, make the process that the concentration of branched-chain saturated hydrocarbon compound increases simultaneously.
This operating condition is preferably to meet the concentration reducing straight chain saturation alkane compound with the condition of the relation of following formula (1).
Concentration >=1.8 of the concentration/straight chain saturation alkane compound of branched-chain saturated hydrocarbon compound ... (1)
Water vapor pyrolysis device 13 is connected to petroleum naphtha isomerization (Isomerization) conversion unit 12, makes water vapor contact with the naphtha fraction processed through petroleum naphtha isomerization (Isomerization) conversion unit 12 and carry out thermolysis.
Then, the thermolysis gas obtained by thermolysis is refined by water vapor pyrolysis device 13, obtains the basic chemical feedstock such as monocyclic aromatic such as desired ethene, propylene, divinyl, benzene.
Butane isomerization (Isomerization) conversion unit 14 is reduced and make the equipment that the concentration of Trimethylmethane increases the concentration of the normal butane refined by crude oil or natural-gas in the butane that obtains.
Then, the butane processed is supplied to water vapor pyrolysis device 13 by butane isomerization (Isomerization) conversion unit 14.Should illustrate, the supply to water vapor pyrolysis device 13 of Trimethylmethane, water vapor pyrolysis device 13 can be supplied to after mixing with the petroleum naphtha processed with petroleum naphtha isomerization (Isomerization) conversion unit 12, also Trimethylmethane directly can be supplied to water vapor pyrolysis device 13.
Foldback mechanism 15 is connected between petroleum naphtha isomerization (Isomerization) conversion unit 12 and water vapor pyrolysis device 13, recovery residues in the straight chain saturation alkane compound in the naphtha fraction of petroleum naphtha isomerization (Isomerization) conversion unit 12 process, and is returned to the equipment of petroleum naphtha isomerization (Isomerization) conversion unit 12.
Petroleum naphtha mixed organization 16 mixes the naphtha fraction without the process of petroleum naphtha isomerization (Isomerization) conversion unit 12 in the naphtha fraction processed through petroleum naphtha isomerization (Isomerization) conversion unit 12.
Should illustrate, as the naphtha fraction processed without petroleum naphtha isomerization (Isomerization) conversion unit 12, can be such as through impurity removal device 11 process those.
(running of ethene manufacturing installation)
Then, for the adjustment of the manufacture of the ethene in above-mentioned ethene manufacturing installation 10 and basic chemical feedstock, such as described belowly to implement.
Namely, naphtha fraction is supplied to after impurity removal device 11 removes impurity, with petroleum naphtha isomerization (Isomerization) conversion unit 12, change the ratio relative to the concentration of the branched-chain saturated hydrocarbon compound of the concentration of the straight chain saturation alkane compound in naphtha fraction, preferably change to the ratio of more than 2.
On the other hand, butane isomerization (Isomerization) conversion unit 14 is supplied to by being refined the butane obtained by crude oil or natural-gas.
Then, the butane processed through butane isomerization (Isomerization) conversion unit 14 is supplied to water vapor pyrolysis device 13.
The naphtha fraction water vapor pyrolysis device 13 being mixed with butane is carried out thermolysis together with water vapor, manufactures ethene and basic chemical feedstock.
Here, increasing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, such as, foldback is carried out by foldback mechanism 15.
On the other hand, reducing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, such as, mixing the naphtha fraction without the process of petroleum naphtha isomerization (Isomerization) conversion unit 12 by petroleum naphtha mixed organization 16.
(action effect of the first embodiment)
As mentioned above, in the above-described first embodiment, reduce the concentration of the straight chain saturation alkane compound in naphtha fraction with petroleum naphtha isomerization (Isomerization) conversion unit 12 after, with water vapor pyrolysis device 13, water vapor contacted and carry out thermolysis.
Therefore, relative to the growing amount of ethene, the ratio of the growing amount of the basic chemical feedstock such as monocyclic aromatic hydrocarbon such as the propylene of the by product of the manufacture as ethene, divinyl, benzene can be increased.Thus, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
Then, in above-mentioned first embodiment, by carrying out isomerization process to naphtha fraction, the concentration of straight chain saturation alkane compound being reduced, makes the concentration of branched-chain saturated hydrocarbon compound increase simultaneously.
Therefore, the ratio of growing amount relative to the growing amount of ethene of basic chemical feedstock can be increased further, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope, the needs of ethene and basic chemical feedstock and the balance of supply can be realized well.
And then, in above-mentioned first embodiment, make the relative concentration of branched-chain saturated hydrocarbon compound in the ratio of the concentration of straight chain saturation alkane compound be more than 2.
Therefore, the ratio of growing amount relative to the growing amount of ethene of basic chemical feedstock can be increased further, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in above-mentioned first embodiment, reclaimed the straight chain saturation alkane compound residued in the naphtha fraction of petroleum naphtha isomerization (Isomerization) conversion unit 12 process by foldback mechanism 15, and be again returned to petroleum naphtha isomerization (Isomerization) conversion unit 12 and process.
Therefore, the concentration of the straight chain saturation alkane compound in the naphtha fraction being supplied to water vapor pyrolysis device 13 can be reduced further, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
And then, in above-mentioned first embodiment, by petroleum naphtha mixed organization 16, in the naphtha fraction processed through petroleum naphtha isomerization (Isomerization) conversion unit 12, suitable mixing is without the naphtha fraction of petroleum naphtha isomerization (Isomerization) conversion unit 12 process, makes the suitable increase of the concentration reduced of straight chain saturation alkane compound.
Therefore, the growing amount of ethene can be made when not changing the growing amount of basic chemical feedstock to increase, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in above-mentioned first embodiment, by butane isomerization (Isomerization) conversion unit 14, the concentration of being refined the normal butane of the butane obtained by crude oil or natural-gas is reduced the concentration of Trimethylmethane is increased, and be mixed in water vapor pyrolysis device 13.
Therefore, easily the concentration of the straight chain saturation alkane compound in naphtha fraction can being reduced, the growing amount of ethene can be reduced when not changing the growing amount of basic chemical feedstock.
Then, in above-mentioned first embodiment, in butane isomerization (Isomerization) conversion unit 14, isomerization process is carried out to butane and the concentration of normal butane is reduced, make the concentration of Trimethylmethane increase simultaneously.
Therefore, easily can increase the concentration of branched-chain saturated hydrocarbon compound, the concentration of the straight chain saturation alkane compound in the naphtha fraction processed with water vapor pyrolysis device 13 can be reduced and increase the concentration of branched-chain saturated hydrocarbon compound, the growing amount of ethene can also be made when not changing the growing amount of basic chemical feedstock to increase, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
［ the second embodiment ］
Then, be described with reference to second embodiment of Fig. 2 to the manufacturing installation of ethene of the present invention.Fig. 2 is the block diagram of the schematic configuration of the ethene manufacturing installation that the second embodiment is shown.Should illustrate, for the formation identical with above-mentioned first embodiment, give identical symbol and omit or simplified illustration.
(formation of ethene manufacturing installation)
As shown in Figure 2, ethene manufacturing installation 20 possesses: the naphtha distillation tower 21 as petroleum naphtha treatment facility, the butane distillation tower 22 as butane treatment equipment, with water vapor pyrolysis device 13.
Naphtha distillation tower 21 distills naphtha fraction, is separated branched-chain saturated hydrocarbon compound and is supplied to water vapor pyrolysis device 13.
Naphtha distillation tower 21 distills such as naphtha fraction.This operating condition identically with the first embodiment, preferably make the relative concentration of branched-chain saturated hydrocarbon compound in the ratio of the concentration of straight chain saturation alkane compound be more than 2.
Butane distillation tower 22 is separated and reclaims the Trimethylmethane refined by crude oil in the butane obtained, with the branched-chain saturated hydrocarbon compound obtained with naphtha distillation tower 21.
Butane distillation tower 22 distills such as butane.
Then, the Trimethylmethane of recovery is mixed in water vapor pyrolysis device 13 by butane distillation tower 22.
(running of ethylene unit)
Then, for the adjustment of the manufacture of the ethene in above-mentioned ethene manufacturing installation 20 and basic chemical feedstock, such as described belowly to implement.
That is, naphtha fraction is supplied to naphtha distillation tower 21, distills, reclaim branched-chain saturated hydrocarbon compound, be supplied to the water vapor pyrolysis device 13 of back segment.
On the other hand, being supplied to butane distillation tower 22 by refining by crude oil or natural-gas the butane obtained, distilling, reclaim Trimethylmethane.
Then, for the branched-chain saturated hydrocarbon compound reclaimed with naphtha distillation tower 21, the Trimethylmethane that mixing is reclaimed with butane distillation tower 22.
Then, carry out with water vapor pyrolysis device 13 thermolysis utilizing water vapor, make ethene and basic chemical feedstock.
Here, increasing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, relative to the branched-chain saturated hydrocarbon compound reclaimed with naphtha distillation tower 21, the ratio of the mixing of the Trimethylmethane reclaimed with butane distillation tower 22 is increased.
On the other hand, reducing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, for branched-chain saturated hydrocarbon compound, the ratio of the mixing of the Trimethylmethane reclaimed with butane distillation tower 22 is reduced.
(action effect of the second embodiment)
As mentioned above, in the above-described 2nd embodiment, reclaim branched-chain saturated hydrocarbon compound with naphtha distillation tower 21 and be supplied to water vapor pyrolysis device 13, thus identically with the first embodiment, the naphtha fraction reducing the state of the concentration of straight chain saturation alkane compound contacted with water vapor by water vapor pyrolysis device 13 and carry out the formation of thermolysis.
Therefore, relative to the growing amount of ethene, the ratio of the growing amount of the basic chemical feedstock such as monocyclic aromatic hydrocarbon such as the propylene of the by product of the manufacture as ethene, divinyl, benzene can be increased.Thus, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
Then, in above-mentioned second embodiment, naphtha fraction is distilled and the branched-chain saturated hydrocarbon compound of separation is supplied to water vapor pyrolysis device 13.
Therefore, the ratio of growing amount relative to the growing amount of ethene of basic chemical feedstock can be increased further, the balance of the growing amount of ethene and basic chemical feedstock can be adjusted in more wide in range scope.
In addition, in above-mentioned second embodiment, butane is distilled and the Trimethylmethane of separation is mixed in the naphtha fraction processed through naphtha distillation tower 21.
Therefore, can straight chain saturation alkane compound easily in the naphtha fraction that processes of reduction water vapor pyrolysis device 13 concentration and increase the concentration of branched-chain saturated hydrocarbon compound.
［ the 3rd embodiment ］
Then, be described with reference to the 3rd embodiment of Fig. 3 to the manufacturing installation of ethene of the present invention.Fig. 3 is the block diagram of the schematic configuration of the ethene manufacturing installation that the 3rd embodiment is shown.Should illustrate, for the formation identical with the second embodiment with above-mentioned first embodiment, give identical symbol and omit or simplified illustration.
(formation of ethene manufacturing installation)
As shown in Figure 3, ethene manufacturing installation 30 possesses: as the middle runnings feed mechanism 31 of petroleum naphtha treatment facility, with water vapor pyrolysis device 13.
Middle runnings feed mechanism 31, by such as boiling point being more than 30 DEG C and the middle runnings of less than 180 DEG C is mixed in naphtha fraction, makes the concentration of the straight chain saturation alkane compound in naphtha fraction reduce.
Such middle runnings specifies above concentration by least wantonly 1 various the reaching in cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound, and this middle runnings is mixed in naphtha fraction, the concentration of the straight chain saturation alkane compound in naphtha fraction is reduced.
Then, middle runnings is mixed in naphtha fraction by middle runnings feed mechanism 31.
Particularly, identically with the second embodiment with above-mentioned first embodiment, the ratio of the concentration of the branched-chain saturated hydrocarbon compound of the concentration relative to the straight chain saturation alkane compound in naphtha fraction is preferably made to be more than 2.
(running of ethene manufacturing installation)
Then, for the adjustment of the manufacture of the ethene in above-mentioned ethene manufacturing installation 30 and basic chemical feedstock, such as described belowly to implement.
That is, by middle runnings feed mechanism 31, boiling point is more than 30 DEG C and the middle runnings of less than 180 DEG C is mixed in naphtha fraction, and is supplied to the water vapor pyrolysis device 13 of back segment.
Then, increasing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, the ratio of the mixing of middle runnings is increased.
On the other hand, reducing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, the ratio of the mixing of middle runnings is reduced.
(action effect of the 3rd embodiment)
As mentioned above, in above-mentioned 3rd embodiment, boiling point is more than 30 DEG C and the middle runnings of less than 180 DEG C is mixed in naphtha fraction, and be supplied to the water vapor pyrolysis device 13 of back segment, thus identically with the second embodiment with the first embodiment, the naphtha fraction reducing the state of the concentration of straight chain saturation alkane compound contacted with water vapor by water vapor pyrolysis device 13 and carry out the formation of thermolysis.
Therefore, relative to the growing amount of ethene, the ratio of the growing amount of the basic chemical feedstock such as monocyclic aromatic hydrocarbon such as the propylene of the by product of the manufacture as ethene, divinyl, benzene can be increased.Thus, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
In addition, in above-mentioned 3rd embodiment, mix more than 30 DEG C and the middle runnings of less than 180 DEG C, thus can mix at least wantonly 1 in ring-type saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound in naphtha fraction, easily can reduce the concentration of the straight chain saturation alkane compound in naphtha fraction.
［ the 4th embodiment ］
Then, be described with reference to the 4th embodiment of Fig. 4 to the manufacturing installation of ethene of the present invention.Fig. 4 is the block diagram of the schematic configuration of the ethene manufacturing installation that the 4th embodiment is shown.Should illustrate, for the formation identical with the respective embodiments described above, give identical symbol and omit or simplified illustration.
(formation of ethene manufacturing installation)
As shown in Figure 4, ethene manufacturing installation 40 possesses: as petroleum naphtha treatment facility straight chain saturation alkane adsorption separation device 41, with water vapor pyrolysis device 13.
Straight chain saturation alkane compound in straight chain saturation alkane adsorption separation device 41 fractionation by adsorption naphtha fraction, reduces the concentration of straight chain saturation alkane compound thus.
This straight chain saturation alkane adsorption separation device 41 uses such as zeolite to carry out fractionation by adsorption straight chain saturation alkane compound.
Should illustrate, as zeolite, such as United States Patent (USP) No. 6407301 zeolite shown in specification sheets can be utilized aptly.In addition, be not limited to use zeolite, also can use can any sorbing material of fractionation by adsorption straight chain saturation alkane compound.
Then, the fractionation by adsorption of straight chain saturation alkane compound, identically with the respective embodiments described above, preferably makes the ratio of the concentration of the branched-chain saturated hydrocarbon compound of the concentration relative to the straight chain saturation alkane compound in naphtha fraction be more than 2.
(running of ethene manufacturing installation)
Then, for the adjustment of the manufacture of the ethene in above-mentioned ethene manufacturing installation 40 and basic chemical feedstock, such as described belowly to implement.
That is, ethene cut is supplied to straight chain saturation alkane adsorption separation device 41, fractionation by adsorption straight chain saturation alkane compound.Then, the naphtha fraction after fractionation by adsorption straight chain saturation alkane compound is supplied to the water vapor pyrolysis device 13 of back segment.
Here, increasing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, to increase the mode of the amount of the straight chain saturation alkane compound of fractionation by adsorption to adjust flow.
On the other hand, reducing in the situation relative to the turnout of the basic chemical feedstock of the turnout of ethene, to reduce the mode of the amount of the straight chain saturation alkane compound of fractionation by adsorption to adjust flow.
(action effect of the 4th embodiment)
As mentioned above, in above-mentioned 4th embodiment, by straight chain saturation alkane adsorption separation device 41, straight chain saturation alkane compound in fractionation by adsorption naphtha fraction, thus identically with the respective embodiments described above, the naphtha fraction reducing the state of the concentration of straight chain saturation alkane compound contacted with water vapor by water vapor pyrolysis device 13 and carry out the formation of thermolysis.
Therefore, relative to the growing amount of ethene, the ratio of the growing amount of the basic chemical feedstock such as monocyclic aromatic hydrocarbon such as the propylene of the by product of the manufacture as ethene, divinyl, benzene can be increased.Thus, even if correspond to requirement and the growing amount of ethene is reduced, also can guarantee the growing amount of basic chemical feedstock, the feed rate of basic chemical feedstock and the balance of requirement can be guaranteed.
In addition, in above-mentioned 4th embodiment, by fractionation by adsorption, the concentration of straight chain saturation alkane compound is reduced, thus easily efficiency can reduce the concentration of straight chain saturation alkane compound well.
And then in above-mentioned 4th embodiment, use zeolite carrys out the straight chain saturation alkane compound in fractionation by adsorption naphtha fraction.
Therefore can easily efficiency fractionation by adsorption straight chain saturation alkane compound well, reduce the concentration of straight chain saturation alkane compound.
［ variation ］
Should illustrate, be disclosed in above record for the formation etc. implementing the best of the present invention, but the present invention be not limited thereto.Namely, the present invention relates generally to specific embodiment and is illustrated, but when not departing from the scope of technological thought of the present invention and object, for above-described embodiment, those skilled in the art can apply various distortion in material, quantity, other detailed formation.
So, the above-mentioned disclosed record limiting material, layer formation etc. is recorded illustratively in order to easy understand the present invention, do not limit the present invention, the record therefore eliminating the title of the restriction of part or all of the restriction of these materials etc. is also contained in the present invention.
Such as, in the first embodiment, butane isomerization (Isomerization) conversion unit 14 also can not be set.
Then, also can substitute petroleum naphtha isomerization (Isomerization) conversion unit 12, and be set to cerebrol distillation tower 21, or be set to straight chain saturation alkane adsorption separation device 41.In the same manner, also can substitute butane isomerization (Isomerization) conversion unit 14, and be set to butane distillation tower 22, or be set to and adsorb and remove the formation of normal butane.
In addition, foldback mechanism 15, petroleum naphtha mixed organization 16 also can not be set.On the other hand, also foldback mechanism 15 or petroleum naphtha mixed organization 16 can be set at ethene manufacturing installation 20,40.
Embodiment
Then, the present invention is specifically described further based on embodiment.
Should illustrate, the present invention does not limit by following examples and comparative example.
［ embodiment 1 ］
Employ and make water vapor contact naphtha fraction and carry out the water vapor pyrolysis device 13 shown in Fig. 5 of thermolysis.The internal diameter of the decomposition pipe 13A of water vapor pyrolysis device 13 is 38mm, length dimension is 10.5m.
Then, as raw material, employ carbonatoms be 4 to 7 straight chain saturation alkane and the single component (normal butane, Trimethylmethane, Skellysolve A, iso-pentane, normal hexane, isohexane, normal heptane, isoheptane) of each carbonatoms decomposing stable hydrocarbon mix those.
Operating condition in water vapor pyrolysis device 13, as shown in the following Table 1, is set to 600 DEG C, decomposes the temperature of pipe outlet 13C and be set to 865 DEG C, decompose the pressure of tube inlet 13B and be set to 1.5kg/cm by the temperature of decomposing tube inlet 13B
2, decompose pipe outlet 13C pressure be set to 1.0kg/cm
2, make that the flow of raw material is 149.5kg/h, the flow of dilution water steam is that 67.28kg/h circulates, carry out thermal decomposition process.
Then, the decomposition gas obtained is distilled, measure the yield of each composition by the thermal decomposition process in water vapor pyrolysis device 13.The results are shown in table 2.
[table 1]
。
[table 2]
。
［ embodiment 2 ］
Then, use the water vapor pyrolysis device 13 shown in Fig. 5, use the composition of each carbonatoms of straight chain saturation alkane and branched-chain saturated hydrocarbon as raw material, measure the turnout of propylene when producing ethene 100t, divinyl, benzene.The results are shown in table 3.
[table 3]
。
According to these experimental results, the turnout obviously confirming the basic chemical feedstock as by product of branched-chain saturated hydrocarbon one side is many.It can thus be appreciated that during supply capacity far below device of the needs of such as ethene, by adopting the raw material being rich in branched-chain saturated hydrocarbon, can reduce the production of ethene as required, simultaneous altitude maintains the production of useful basic chemical feedstock.
Nomenclature
10,20,30,40 ... ethene manufacturing installation
12 ... as petroleum naphtha isomerization (Isomerization) conversion unit of petroleum naphtha treatment facility
13 ... water vapor pyrolysis device
14 ... as butane isomerization (Isomerization) conversion unit of butane treatment equipment
15 ... foldback mechanism
16 ... petroleum naphtha mixed organization
21 ... as the naphtha distillation tower of petroleum naphtha treatment facility
22 ... as the butane distillation tower of butane treatment equipment
31 ... as the middle runnings feed mechanism of petroleum naphtha treatment facility
41 ... as the straight chain saturation alkane adsorption separation device of petroleum naphtha treatment facility.
Claims (15)
1. the manufacturing installation of ethene, it naphtha fraction is carried out thermolysis together with water vapor and manufactures the manufacturing installation of the ethene of ethene, it is characterized in that possessing:
By the petroleum naphtha treatment facility that the concentration of the straight chain saturation alkane compound in described naphtha fraction reduces; With
Described naphtha fraction through the process of described petroleum naphtha treatment facility is carried out together with water vapor the water vapor pyrolysis device of thermolysis.
2. the manufacturing installation of ethene according to claim 1, is characterized in that,
Described petroleum naphtha treatment facility carries out isomerization process to described naphtha fraction and the concentration of described straight chain saturation alkane compound is reduced, and makes the concentration of branched-chain saturated hydrocarbon compound increase simultaneously.
3. the manufacturing installation of ethene according to claim 1, is characterized in that,
Described petroleum naphtha treatment facility distills described naphtha fraction and the branched-chain saturated hydrocarbon compound of separation is supplied to described water vapor pyrolysis device.
4. the manufacturing installation of ethene according to claim 1, is characterized in that,
Described straight chain saturation alkane compound in naphtha fraction described in described petroleum naphtha treatment facility fractionation by adsorption and the concentration of described straight chain saturation alkane compound is reduced.
5. the manufacturing installation of ethene according to claim 4, is characterized in that,
Described petroleum naphtha treatment facility uses zeolite to carry out straight chain saturation alkane compound described in fractionation by adsorption.
6. the manufacturing installation of ethene according to claim 1, is characterized in that,
In cyclic saturated hydrocarbon compound, aromatic hydrocarbon compound and unsaturated hydrocarbon compound at least wantonly 1 is mixed in described naphtha fraction by described petroleum naphtha treatment facility, the concentration of the straight chain saturation alkane compound in described naphtha fraction is reduced.
7. the manufacturing installation of ethene according to claim 6, is characterized in that,
The boiling point of described cyclic saturated hydrocarbon compound is more than 49 DEG C and less than 160 DEG C,
The boiling point of described aromatic hydrocarbon compound is more than 80 DEG C and less than 160 DEG C.
8. the manufacturing installation of the ethene described in claim 6 or 7, is characterized in that,
Boiling point is more than 30 DEG C to described petroleum naphtha treatment facility and the middle runnings of less than 180 DEG C is mixed in described naphtha fraction.
9. the manufacturing installation of the ethene according to any one of claim 1 to 8, is characterized in that,
Described petroleum naphtha treatment facility reduces the concentration of described straight chain saturation alkane compound with the condition of the relation of following formula (1) to meet:
Concentration >=1.8 of the concentration/straight chain saturation alkane compound of branched-chain saturated hydrocarbon compound ... (1).
10. the manufacturing installation of the ethene according to any one of claim 1 to 9, is characterized in that,
Possess: the straight chain saturation alkane compound residued in the naphtha fraction of described petroleum naphtha treatment facility process is reclaimed and is returned to the foldback mechanism of described petroleum naphtha treatment facility.
The manufacturing installation of the ethene according to any one of 11. claims 1 to 10, is characterized in that,
Possess: the petroleum naphtha mixed organization mixing the naphtha fraction without the process of described petroleum naphtha treatment facility in the naphtha fraction through the process of described petroleum naphtha treatment facility.
The manufacturing installation of the ethene according to any one of 12. claims 1 to 11, is characterized in that,
Possessing the concentration reduction making to be refined by crude oil or natural-gas the normal butane in the butane obtained makes the concentration of Trimethylmethane increase, and is supplied to the butane treatment equipment of described water vapor pyrolysis device.
The manufacturing installation of 13. ethene according to claim 12, is characterized in that,
Described butane treatment equipment carries out isomerization process to described butane and the concentration of normal butane is reduced, and makes the concentration of Trimethylmethane increase simultaneously.
The manufacturing installation of 14. ethene according to claim 12, is characterized in that,
Described butane treatment equipment distills described butane and the Trimethylmethane of separation is supplied to described water vapor pyrolysis device.
The manufacture method of 15. ethene, it naphtha fraction is carried out thermolysis together with water vapor and manufactures the manufacture method of the ethene of ethene, it is characterized in that, implements:
By the petroleum naphtha treatment step that the concentration of the straight chain saturation alkane compound in described naphtha fraction reduces; With
The naphtha fraction processed in described petroleum naphtha treatment step is carried out together with water vapor the water vapor thermal decomposition steps of thermolysis.
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| JP2013048987A JP2014172887A (en) | 2013-03-12 | 2013-03-12 | Apparatus and method for producing ethylene |
| JP2013-048987 | 2013-03-12 | ||
| PCT/JP2014/055806 WO2014142002A1 (en) | 2013-03-12 | 2014-03-06 | Apparatus and method for producing ethylene |
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| KR (1) | KR20150125660A (en) |
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| WO2018114866A1 (en) * | 2016-12-20 | 2018-06-28 | Sandvik Intellectual Property Ab | Tube arrangement and furnace |
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| JP2014172887A (en) | 2014-09-22 |
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Application publication date: 20151104 |