CN219689638U - System for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar - Google Patents
System for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar Download PDFInfo
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- CN219689638U CN219689638U CN202320332536.8U CN202320332536U CN219689638U CN 219689638 U CN219689638 U CN 219689638U CN 202320332536 U CN202320332536 U CN 202320332536U CN 219689638 U CN219689638 U CN 219689638U
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- 239000011280 coal tar Substances 0.000 title claims abstract description 96
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 51
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 43
- 239000002904 solvent Substances 0.000 title claims abstract description 30
- 238000005194 fractionation Methods 0.000 claims abstract description 104
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 56
- 238000007599 discharging Methods 0.000 claims abstract description 39
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 239000003350 kerosene Substances 0.000 claims abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- 238000005261 decarburization Methods 0.000 claims abstract description 11
- 238000005262 decarbonization Methods 0.000 claims abstract description 10
- 238000002407 reforming Methods 0.000 claims description 37
- 230000003197 catalytic effect Effects 0.000 claims description 12
- 238000004939 coking Methods 0.000 claims description 12
- 238000001833 catalytic reforming Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 239000011294 coal tar pitch Substances 0.000 claims description 10
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 229910052717 sulfur Inorganic materials 0.000 claims description 5
- 125000005842 heteroatom Chemical group 0.000 claims description 4
- ISWSIDIOOBJBQZ-UHFFFAOYSA-M phenolate Chemical compound [O-]C1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-M 0.000 claims 1
- 229940031826 phenolate Drugs 0.000 claims 1
- 239000002283 diesel fuel Substances 0.000 abstract description 9
- 239000003921 oil Substances 0.000 description 57
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 33
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 33
- 239000000047 product Substances 0.000 description 30
- 238000000034 method Methods 0.000 description 14
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 13
- 238000009835 boiling Methods 0.000 description 13
- 239000007789 gas Substances 0.000 description 12
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 11
- 238000005984 hydrogenation reaction Methods 0.000 description 9
- 239000008096 xylene Substances 0.000 description 9
- 239000000571 coke Substances 0.000 description 5
- -1 monocyclic aromatic hydrocarbons Chemical class 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000011331 needle coke Substances 0.000 description 4
- 238000005336 cracking Methods 0.000 description 3
- 238000005520 cutting process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 150000003738 xylenes Chemical class 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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Abstract
The utility model discloses a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar, which comprises a decarbonization device, a fraction separation device, a hydrofining device, a first fractionation device, a hydrocracking device and a second fractionation device; the fraction separating device comprises a first feeding end and a first discharging end; the first fractionating device is connected with the hydrofining device; the hydrocracking device is connected with the first fractionating device and the second fractionating device; the second fractionating device is connected with the hydrocracking device. According to the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, disclosed by the utility model, carbon and separation components are removed through the decarburization device and the fraction separation device, the mixed fraction enters the hydrofining device and the hydrocracking device, light naphtha, heavy naphtha, aviation kerosene, white oil and high-cetane-number diesel oil are separated through the first fractionation device, and the full fraction of the medium-temperature coal tar is fully utilized, so that a product with high added value is obtained, the utilization value of the medium-temperature coal tar is improved, and the system has a good application prospect.
Description
Technical Field
The utility model belongs to the technical field of coal tar processing equipment, and particularly relates to a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar.
Background
Coal tar is a liquid byproduct generated in the coal deep processing process, has pungent smell, and can be divided into low-temperature coal tar, medium-temperature coal tar and high-temperature coal tar according to different pyrolysis temperatures. Coal tar has a complex composition, contains a large amount of polycyclic aromatic hydrocarbon, S, N, O and other heteroatoms, and metal and other non-hydrocarbon compounds, and is mainly processed and utilized by a hydrogenation process at present. Coal tar hydrogenation technology is the most rational and effective key technology. The coal tar hydro-upgrading process can be roughly divided into two parts: hydrofinishing and hydrocracking. The hydrofining part is mainly used for removing sulfur, nitrogen, oxygen, heavy metals and other impurity molecules in the coal tar, is a main reaction in the coal tar hydrogenation upgrading process, and determines whether the product meets the subsequent production requirements or not according to the quality of hydrofining. The purpose of hydrocracking is to produce light fuel oil hydrogenation process by alkane cracking, naphthene cracking, arene cracking and other reactions of coal tar under the actions of high temperature and high pressure, catalyst and hydrogen. At present, the medium-temperature coal tar mainly produces aromatic hydrocarbon by a method combining hydrofining and hydrocracking, so that the high-efficiency utilization of coal tar resources is realized.
There are two technical solutions for utilizing coal tar in the prior art. The method is to produce light diesel oil by hydrofining coal tar hydrogenated distillate oil as a raw material, and then produce mixed aromatic hydrocarbon by hydrocracking and reforming. The technical scheme mainly has the following technical defects:
(1) The mixed aromatic hydrocarbon is produced by taking partial coal tar hydrogenation distillate oil as a raw material, the whole coal tar distillate is not fully utilized, and the comprehensive economy is low;
(2) The product mixed aromatic hydrocarbon prepared by utilizing partial coal tar hydrogenation fraction is not effectively separated and purified, and the added value of the product is required to be further improved.
And the other is to take the whole fraction of the medium-low temperature coal tar as a raw material, pretreat and fractionate, then crack and refine the light phase, crack the heavy phase twice and refine and crack the heavy phase, and finally realize the hydrogenation of the whole fraction coal tar to prepare monocyclic aromatic hydrocarbons such as benzene, toluene, xylene and the like. The technical scheme mainly has the following technical defects:
the medium-low temperature coal tar is only subjected to hydrofining and hydrocracking to produce benzene, toluene, xylene and other monocyclic aromatic hydrocarbon, the product structure is single, and the coal tar is not subjected to scientific chemical cutting so as to realize the production of aromatic hydrocarbon, alkane and other products by the coal tar.
Disclosure of Invention
The embodiment of the utility model provides a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar, which can fully utilize the full fraction of the medium-temperature coal tar to obtain a product with high added value, has low production cost, extends the coal tar hydrogenation industry chain, improves the utilization value of the medium-temperature coal tar and has better application prospect.
In a first aspect, the utility model provides a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar, which comprises a decarbonization device 1, a fraction separation device 2, a hydrofining device 3, a first fractionation device 4, a hydrocracking device 5 and a second fractionation device 6;
the fraction separation device 2 comprises a first feeding end 201 and a first discharging end 202, the first feeding end 201 is connected with the decarburization device 1, and the first discharging end 202 is connected with the hydrofining device 3; the first fractionation feed end 401 of the first fractionation unit 4 is connected to the hydrorefining unit 3;
the decarbonization device 1 is used for removing carbon in medium-temperature coal tar serving as a raw material; the fraction separation device 2 is used for separating fractions from the medium-temperature coal tar from which carbon is removed; the hydrofining device 3 is used for removing S, N heteroatoms contained in the mixed fraction to obtain a hydrofining product; a first fractionation device 4 for separating the hydrofinished product;
the hydrocracking feeding end 500 of the hydrocracking device 5 is respectively connected with the first fraction device 4 and the second fraction device 6, and is used for hydrocracking tail oil separated by the first fraction device 4 and heavy components separated by the second fraction device 6; the second fractionation device 6 is connected to the hydrocracking device 5 at its second fractionation feed end 601 for separating cracked products. The second fractionation device 6 is used for separating second rich gas, light naphtha, heavy naphtha, aviation kerosene, white oil, high cetane number diesel oil and heavy components from the hydrocracking product.
In one embodiment of the present utility model, the system for producing aromatic hydrocarbon and alkane solvent oil from medium temperature coal tar further comprises:
and the reforming device 7 is connected with the reforming feed end 700 of the reforming device 7 and the first fractionating device 4 and the second fractionating device 6 respectively and is used for carrying out catalytic reforming on the light components separated by the first fractionating device 4 and the heavy naphtha separated by the second fractionating device 6 so as to obtain a catalytic reforming product containing polyaromatics.
In an embodiment of the present utility model, the system for producing aromatic hydrocarbon and alkane solvent oil from medium temperature coal tar further comprises:
dewaxing unit 8, which is connected to reforming unit 7, is used for removing alkane component in the catalytic reformate.
According to the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, the medium-temperature coal tar is used as a raw material, carbon, medium-temperature coal tar pitch, phenol oil and rich gas are removed through the decarburization device and the fraction separation device, the rest mixed fraction sequentially enters the hydrofining device, the first fractionation device and the hydrocracking device, and the components such as light naphtha, aviation kerosene, white oil, high-cetane diesel oil and heavy petroleum oil are separated through the first fractionation device, so that the fraction of the medium-temperature coal tar is utilized more completely.
The heavy naphtha can further enter a reforming device for reforming to obtain a catalytic reforming product, alkane is removed from the catalytic reforming product through a dewaxing device, benzene, toluene, xylene and high-boiling aromatic hydrocarbon are separated through a third fractionation device, and mixed aromatic hydrocarbon is produced by using medium-temperature coal tar through a series of devices which are sequentially connected, so that each component of the medium-temperature coal tar is subjected to scientific 'chemical cutting', the whole fraction of the medium-temperature coal tar is fully utilized, and the comprehensive economy of the medium-temperature coal tar is improved. Solves the problems that the product structure is single and other components of the coal tar are not reasonably utilized because only hydrofining and hydrocracking are carried out on the medium-temperature coal tar to produce the monocyclic aromatic hydrocarbon.
In one embodiment of the present utility model, the decarbonization device 1 comprises a coking tower 100, wherein the coking tower 100 is used for removing carbon in the medium temperature coal tar, namely, removing heavy components in the medium temperature coal tar through the coking tower 100 to produce coke.
In one embodiment of the utility model, the fraction separation device 2 comprises a fraction column 200, the first feed end 201 of the fraction column 200 being connected to the decarbonization device 1. Specifically, the first feeding end 201 of the distillation column 200 is connected to the first discharging end 202 of the coking tower 100, and the first discharging end 202 of the distillation column 200 includes a rich gas discharging end 202a, a phenol oil fraction discharging end 202b, a mixed fraction discharging end 202c, and a medium temperature coal tar pitch discharging end 202d. Wherein, the phenol oil fraction can be used for separating and purifying phenol products, the medium-temperature coal tar pitch can be used for producing needle coke, and the mixed fraction enters a mixed fraction hydrofining device.
In one embodiment of the present utility model, the hydrofining apparatus 3 is provided with a hydrofining feed end 300 and a hydrofining discharge end 301, wherein the hydrofining feed end 300 is connected with the fraction separating apparatus 2, and the hydrofining discharge end 301 of the hydrofining apparatus is connected with the first fractionating apparatus 4. Specifically, the hydrofining feed end 300 of the hydrofining feed device 3 is connected to the mixed fraction discharge end 202c of the fraction tower 200, and the hydrofining discharge end 301 of the hydrofining feed device 3 is connected to the first fractionation feed end 401 of the first fractionation device 4.
In one embodiment of the present utility model, the first fractionation unit 4 includes a first fractionation column 400, a first fractionation feed end 401 of the first fractionation column 400 is connected to the hydrofining unit 3, and a first fraction discharge end 402 of the first fractionation column 400 is connected to the hydrocracking unit 5 and the reforming unit 7, respectively. Specifically, the first fractionation feed end 401 of the first fractionation column 400 is connected to the hydrofining discharge end 301 of the hydrofining device 3, the first fraction discharge end 402 includes a light component discharge end 402a and a tail oil discharge end 402b, the light component discharge end 402a is connected to the reforming feed end 700 of the reforming device 7, and the tail oil discharge end 402b is connected to the hydrocracking feed end 500 of the hydrocracking device 5.
In one embodiment of the present utility model, the hydrocracking feed end 500 of the hydrocracking apparatus 5 is connected to a hydrocracking feed supply end which comprises the tail oil discharge end 402b of the first fractionating tower 400 and the heavy component discharge end 6027 of the second fractionating tower 600, respectively, so as to supply the hydrocracking apparatus 5 with the hydrocracked feed.
In one embodiment of the present utility model, the second fractionation device 6 includes a second fractionation column 600, where a second fractionation feed end 601 is connected to the hydrocracking discharge end 501 of the hydrocracking unit 5, and a second fractionation feed end 602 of the second fractionation column 600 includes a second rich gas discharge end 6021, a light naphtha discharge end 6022, a heavy naphtha discharge end 6023, an aviation kerosene discharge end 6024, a white oil discharge end 6025, a high cetane diesel discharge end 6026, and a heavy component discharge end 6027 to produce a second rich gas, a light naphtha, a heavy naphtha, aviation kerosene, white oil, high cetane diesel, and heavy components, respectively.
In one embodiment of the present utility model, the reformer 7 is provided with a reforming feed end 700, and the reforming feed end 700 is connected to a reforming raw material supply end. The reforming feedstock supply ends include a light fraction discharge end 402a of the first fractionation column 400 and a heavy naphtha discharge end 6023 of the second fractionation column 600, respectively.
In one embodiment of the utility model, dewaxing unit 8 is provided with dewaxing feed 800 and dewaxing discharge 801, dewaxing discharge 801 comprising alkane discharge 801a and catalytic reformate discharge 801b for removal of alkane components; the dewaxing unit 8 comprises a third fractionation unit 9 connected to the dewaxing unit 8, the third fractionation unit 9 being configured to separate the catalytic reformate depleted of alkane components to separate benzene, toluene, xylenes and higher boiling aromatics.
In an embodiment of the present utility model, the third fractionation device 9 includes a third fractionation column 900, where the third fractionation column 900 is provided with a third fractionation feed end 901 and a third fractionation discharge end 902, and the third fractionation feed end 901 of the third fractionation column 900 is connected to the dewaxing discharge end 801 of the dewaxing device 8; specifically, the third fractionation feed end 901 is connected to the catalytic reformate discharge end 801b for removal of alkane components; third fractionation output 902 includes benzene output 902a, toluene output 902b, xylene output 902c, and high boiling aromatic hydrocarbon output 902d, respectively. High-boiling aromatics are those whose boiling range is > 140 ℃.
According to the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, after the heavy components are removed from the medium-temperature coal tar through the decarburization device to produce coke so as to achieve coking and decarburization, the coke and the components enter the fraction fractionating device to be separated, needle coke can be further produced from the medium-temperature coal tar pitch and phenol oil in the separated products, phenol products can be separated and purified, and the produced mixed fraction sequentially passes through the hydrofining device, the first fractionating device, the hydrocracking device and the second fractionating device to produce aviation kerosene, white oil, diesel oil with high cetane number, light naphtha, heavy naphtha and heavy components, and fully utilized full fraction of the medium-temperature coal tar can obtain products with high added value.
Furthermore, in the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, the heavy naphtha is subjected to catalytic reforming to produce alkane through the reforming system, benzene, toluene, dimethylbenzene, high-boiling aromatic hydrocarbon and alkane solvent oil are produced through the dewaxing device, the full fraction of the medium-temperature coal tar is further fully utilized, and the comprehensive economy of the coal tar is improved.
Drawings
In order to more clearly illustrate the technical solution of the embodiments of the present utility model, the drawings that are needed to be used in the embodiments of the present utility model will be briefly described, and it is possible for a person skilled in the art to obtain other drawings according to these drawings without inventive effort.
FIG. 1 is a schematic diagram of a system for producing aromatic hydrocarbon and alkane solvent oil from medium temperature coal tar according to an embodiment of the present utility model;
fig. 2 is a schematic structural view of a reformer and dewaxing apparatus according to another embodiment of the present utility model.
Reference numerals illustrate:
1. a decarburization device; 100. a coking tower;
2. fraction separating means; 200. a distillate tower; 201. a first feed end; 202. the first discharging end; 202a, a rich gas discharging end; 202b, a discharging end of the phenol oil fraction; 202c, mixing the distillate discharge end; 202d, a medium-temperature coal tar pitch discharge end;
3. a hydrofining device; 300. hydrofining a feed end; 301. a hydrofining discharge end;
4. a first fractionation device; 400. a first fractionation column; 401. a first fractionation feed end; 402. a first fractionation discharge end; 402a, a light component discharge end; 402b, tail oil discharge end;
5. a hydrocracking unit; 500. hydrocracking a feed end; 501. a hydrocracking discharge end;
6. a second fractionation device; 600. a second fractionation column; 601. a second fractionation feed end; 602. a second split feed end; 6021. a second rich gas discharge end; 6022. a light naphtha discharge end; 6023. a heavy naphtha discharge end; 6024. aviation kerosene discharge end; 6025. a white oil discharge end; 6026. the discharge end of the diesel oil with high cetane number; 6027. and a heavy component discharge end.
7. A reforming device; 700. reforming a feed end; 701. reforming a discharge end;
8. a dewaxing device; 800. dewaxing a feed end; 801. dewaxing a discharge end; 801a, alkane discharging end; 801b, removing alkane components from a discharge end of a catalytic reforming product;
9. a third fractionation device; 900. a third fractionation column; 901. a third fractionation feed end; 902. a third fractionation discharge end; 902a, benzene discharge end; 902b, a toluene discharge end; 902c, a xylene discharge end; 902d, a high boiling point aromatic hydrocarbon discharge end.
Detailed Description
Features and exemplary embodiments of various aspects of the present utility model will be described in detail below, and in order to make the objects, technical solutions and advantages of the present utility model more apparent, the present utility model will be described in further detail below with reference to the accompanying drawings and the detailed embodiments. It should be understood that the particular embodiments described herein are meant to be illustrative of the utility model only and not limiting. It will be apparent to one skilled in the art that the present utility model may be practiced without some of these specific details. The following description of the embodiments is merely intended to provide a better understanding of the utility model by showing examples of the utility model.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising … …" does not exclude the presence of other like elements in a process, method, article or apparatus that comprises the element.
As described in the background section, coal tar distillate is used to produce mixed aromatics, and the coal tar full distillate is not fully utilized. The adoption of medium-temperature coal tar only for hydrofining and hydrocracking to produce monocyclic aromatic hydrocarbon leads to the technical problem that the product structure is single and other components of the coal tar are not reasonably utilized.
In order to solve the problems in the prior art, the embodiment of the utility model provides a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar. The system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar provided by the embodiment of the utility model is first described below.
Fig. 1 shows a schematic structural diagram of a system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar according to an embodiment of the present utility model.
As shown in fig. 1, the system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar comprises a decarbonization device 1, a fraction separation device 2, a hydrofining device 3, a first fractionation device 4, a hydrocracking device 5 and a second fractionation device 6;
the fraction separation device 2 comprises a first feeding end 201 and a first discharging end 202, the first feeding end 201 is connected with the decarburization device 1, and the first discharging end 202 is connected with the hydrofining device 3; the first fractionation feed end 401 of the first fractionation unit 4 is connected to the hydrorefining unit 3;
the decarbonization device 1 is used for removing carbon in medium-temperature coal tar serving as a raw material; the fraction separation device 2 is used for separating fractions from the medium-temperature coal tar from which carbon is removed; the hydrofining device 3 is used for removing S, N heteroatoms contained in the mixed fraction to obtain a hydrofining product; a first fractionation device 4 for separating the hydrofinished product;
the hydrocracking feeding end 500 of the hydrocracking device 5 is respectively connected with the first fraction device 4 and the second fraction device 6, and is used for hydrocracking tail oil separated by the first fraction device 4 and heavy components separated by the second fraction device 6; the second fractionation device 6 is connected to the hydrocracking device 5 at its second fractionation feed end 601 for separating cracked products. The second fractionation device 6 is used for separating second rich gas, light naphtha, heavy naphtha, aviation kerosene, white oil, high cetane number diesel oil and heavy components from the hydrocracking product.
According to the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, the medium-temperature coal tar is used as a raw material, carbon, medium-temperature coal tar pitch, phenol oil and rich gas are removed through the decarburization device and the fraction separation device, the rest mixed fraction sequentially enters the hydrofining device, the first fractionation device and the hydrocracking device, and the components such as light naphtha, aviation kerosene, white oil, high-cetane diesel oil and heavy petroleum oil are separated through the first fractionation device, so that the fraction of the medium-temperature coal tar is utilized more completely.
The system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar comprises a coking tower 100, wherein the medium-temperature coal tar is used for removing heavy components from the coking tower 100 to produce coke, namely the coking tower 100 is used for removing carbon from the medium-temperature coal tar.
In the system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar according to the embodiment of the utility model, the fraction separation device 2 comprises a fraction tower 200, and a first feeding end 201 of the fraction tower 200 is connected with the decarbonization device 1. Specifically, the first feeding end 201 of the distillation column 200 is connected to the discharging end of the coking tower 100, and the first discharging end 202 of the distillation column 200 includes a rich gas discharging end 202a, a phenol oil fraction discharging end 202b, a mixed fraction discharging end 202c, and a medium temperature coal tar pitch discharging end 202d. Wherein, the phenol oil fraction can be used for separating and purifying phenol products, the medium-temperature coal tar pitch can be used for producing needle coke, and the mixed fraction enters a hydrofining device for hydrofining.
According to the system for producing aromatic hydrocarbon and alkane solvent oil from medium-temperature coal tar, a hydrofining device 3 is provided with a hydrofining feeding end 300 and a hydrofining discharging end 301, wherein the hydrofining feeding end 300 is connected with a fraction separating device 2, and the hydrofining discharging end 301 of the hydrofining device is connected with a first fractionating device 4. Specifically, the hydrofining feed end 300 of the hydrofining feed device 3 is connected with the mixed fraction discharge end 202c of the fraction tower 200 to provide the mixed fraction to the hydrofining feed device 3; the hydrofining discharge end 301 of the hydrofining device 3 is connected to the first fractionation feed end 401 of the first fractionation device 4 so that the hydrofined mixed fraction is transferred to the first fractionation device for separation.
In the system for producing aromatic hydrocarbon and alkane solvent naphtha from medium-temperature coal tar according to the embodiment of the utility model, the first fractionating device 4 comprises a first fractionating tower 400, a first fractionating feeding end 401 of the first fractionating tower 400 is connected with the hydrofining device 3, and a first fraction discharging end 402 of the first fractionating tower 400 is respectively connected with the hydrocracking device 5 and the reforming device 7. Specifically, the first fractionation feed end 401 of the first fractionation column 400 is connected to the hydrofining discharge end 301 of the hydrofining device 3, the first fraction discharge end 402 includes a light component discharge end 402a and a tail oil discharge end 402b, the light component discharge end 402a is connected to the reforming feed end 700 of the reforming device 7, and the tail oil discharge end 402b is connected to the hydrocracking feed end 500 of the hydrocracking device 5.
In one embodiment of the present utility model, the hydrocracking feed end 500 of the hydrocracking apparatus 5 is connected to a hydrocracking feed supply end which comprises the tail oil discharge end 402b of the first fractionating tower 400 and the heavy component discharge end 6027 of the second fractionating tower 600, respectively, so as to supply the hydrocracking apparatus 5 with the hydrocracked feed.
In one embodiment of the present utility model, the second fractionation device 6 includes a second fractionation column 600, where a second fractionation feed end 601 is connected to the hydrocracking discharge end 501 of the hydrocracking unit 5, and a second fractionation feed end 602 of the second fractionation column 600 includes a second rich gas discharge end 6021, a light naphtha discharge end 6022, a heavy naphtha discharge end 6023, an aviation kerosene discharge end 6024, a white oil discharge end 6025, a high cetane diesel discharge end 6026, and a heavy component discharge end 6027 to produce a second rich gas, a light naphtha, a heavy naphtha, aviation kerosene, white oil, high cetane diesel, and heavy components, respectively.
The heavy ends discharge end 6027 of the second fraction end 602 is connected to the reforming feed end 700 of the reformer 7.
In this embodiment, as shown in fig. 2, the system for producing aromatic hydrocarbon and alkane solvent oil from medium temperature coal tar further comprises:
a reforming device 7, the reforming feeding end 700 of which is respectively connected with the first fractionating device 4 and the second fractionating device 6, and is used for carrying out catalytic reforming on the light component separated by the first fractionating device 4 and the heavy naphtha separated by the second fractionating device 6 so as to obtain a catalytic reforming product containing polyaromatics;
dewaxing unit 8, which is connected to reforming unit 7, is used for removing alkane component in the catalytic reformate.
The heavy components separated by the second fractionating device and the tail oil separated by the first fractionating device can further enter the reforming device for reforming to obtain a catalytic reformate, the catalytic reformate is subjected to paraffin removal by the dewaxing device, benzene, toluene, xylene and high-boiling aromatic hydrocarbon are separated by the third fractionating device, and mixed aromatic hydrocarbon is produced by using the medium-temperature coal tar through a series of devices which are sequentially connected, so that each component of the medium-temperature coal tar is subjected to scientific 'chemical cutting', the whole fraction of the medium-temperature coal tar is fully utilized, and the comprehensive economy of the medium-temperature coal tar is improved. Solves the problems that the product structure is single and other components of the coal tar are not reasonably utilized because only hydrofining and hydrocracking are carried out on the medium-temperature coal tar to produce the monocyclic aromatic hydrocarbon.
In the system for producing aromatic hydrocarbon and alkane solvent oil by using warm coal tar according to the embodiment of the utility model, the reforming device 7 is provided with a reforming feeding end 700 and a reforming discharging end 701, and the reforming feeding end 700 is connected with a reforming raw material supply end. The reforming feedstock supply ends include a light fraction discharge end 402a of the first fractionation column 400 and a heavy naphtha discharge end 6023 of the second fractionation column 600, respectively.
In the system for producing aromatic hydrocarbon and alkane solvent oil by using warm coal tar, a dewaxing device 8 is provided with a dewaxing feeding end 800 and a dewaxing discharging end 801, wherein the dewaxing feeding end 800 is connected with a light component discharging end 402a of a first fractionating tower 400 and a heavy naphtha discharging end 6023 of a second fractionating tower 600; dewaxing output 801 includes alkane output 801a and catalytic reformate output 801b for removal of alkane components; the dewaxing unit 8 comprises a third fractionation unit 9 connected to the dewaxing unit 8, the third fractionation unit 9 being configured to separate the catalytic reformate depleted of alkane components to separate benzene, toluene, xylenes and higher boiling aromatics.
In an embodiment of the present utility model, the third fractionation device 9 includes a third fractionation column 900, where the third fractionation column 900 is provided with a third fractionation feed end 901 and a third fractionation discharge end 902, and the third fractionation feed end 901 of the third fractionation column 900 is connected to the dewaxing discharge end 801 of the dewaxing device 8; specifically, the third fractionation feed end 901 is connected to the catalytic reformate discharge end 801b for removal of alkane components; third fractionation output 902 includes benzene output 902a, toluene output 902b, xylene output 902c, and high boiling aromatic hydrocarbon output 902d, respectively. High-boiling aromatics are those whose boiling range is > 140 ℃.
According to the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, the medium-temperature coal tar is taken as a raw material, heavy components are removed through the decarburization device to produce coke so as to achieve coking and decarburization, other components enter the fraction fractionating device to be separated, the separated product is subjected to medium-temperature coal tar pitch to further produce needle coke, the phenol oil is used for separating and purifying phenolic products, the produced mixed fraction sequentially passes through the hydrofining device, the first fractionating device, the hydrocracking device and the second fractionating device to produce aviation kerosene, white oil, high-cetane diesel oil, light naphtha, heavy naphtha and heavy components, and the full fraction of the medium-temperature coal tar is fully utilized, so that the product with high added value can be obtained, the production cost is low, the coal tar hydrogenation industry chain is prolonged, the utilization value of the medium-temperature coal tar is improved, and the system has a good application prospect.
Furthermore, in the system for producing aromatic hydrocarbon and alkane solvent oil from the medium-temperature coal tar, the heavy naphtha is subjected to catalytic reforming to produce alkane through the reforming system, benzene, toluene, dimethylbenzene, high-boiling aromatic hydrocarbon and alkane solvent oil are produced through the dewaxing device, the full fraction of the medium-temperature coal tar is further fully utilized, and the comprehensive economy of the coal tar is improved.
In the foregoing, only the specific embodiments of the present utility model are described, and it will be clearly understood by those skilled in the art that, for convenience and brevity of description, the specific working processes of the systems, modules and units described above may refer to the corresponding processes in the foregoing method embodiments, which are not repeated herein. It should be understood that the scope of the present utility model is not limited thereto, and any equivalent modifications or substitutions can be easily made by those skilled in the art within the technical scope of the present utility model, and they should be included in the scope of the present utility model.
Claims (10)
1. The system for producing aromatic hydrocarbon and alkane solvent oil by using medium-temperature coal tar is characterized by comprising a decarbonization device (1), a fraction separation device (2), a hydrofining device (3), a first fractionation device (4), a hydrocracking device (5) and a second fractionation device (6);
the fraction separation device (2) comprises a first feeding end (201) and a first discharging end (202), wherein the first feeding end (201) is connected with the decarburization device (1), and the first discharging end (202) is connected with the hydrofining device (3); a first fractionation feeding end (401) of the first fractionation device (4) is connected with the hydrofining device (3);
the decarbonization device (1) is used for removing carbon in medium-temperature coal tar serving as a raw material; the fraction separation device (2) is used for separating fractions from the medium-temperature coal tar from which the carbon is removed; the hydrofining device (3) is used for removing S, N heteroatoms contained in the mixed fraction to obtain a hydrofining product; said first fractionation means (4) for separating hydrofinished products;
the hydrocracking feeding end (500) of the hydrocracking device (5) is respectively connected with the first fractionating device (4) and the second fractionating device (6), and the hydrocracking device (5) is used for hydrocracking tail oil separated by the first fractionating device (4) and heavy components separated by the second fractionating device (6); and the second fractionating device (6) is connected with the hydrocracking device (5) at a second fractionating feeding end (601) and is used for separating cracked products.
2. The system of claim 1, further comprising:
and the reforming device (7) is connected with the reforming feeding end (700) of the first fractionating device (4) and the second fractionating device (6) respectively and is used for carrying out catalytic reforming on the light components separated by the first fractionating device (4) and the heavy naphtha separated by the second fractionating device (6).
3. The system of claim 2, further comprising:
dewaxing means (8) connected to said reforming means (7) for removing alkane components from the catalytic reformate.
4. A system according to any one of claims 1 to 3, characterized in that the decarbonizing device (1) comprises a coking drum (100).
5. A system according to any one of claims 1 to 3, characterized in that the fraction separation device (2) comprises a fraction column (200), a first feed end (201) of the fraction column (200) being connected to the decarbonizing device (1), a first discharge end (202) of the fraction column (200) comprising a rich gas discharge end (202 a), a phenolate fraction discharge end (202 b), a mixed fraction discharge end (202 c), a medium temperature coal tar pitch discharge end (202 d).
6. A system according to any one of claims 1 to 3, characterized in that the hydrofinishing device (3) is provided with a hydrofinishing feed end (300) and a hydrofinishing discharge end (301); the hydrofining feeding end (300) of the hydrofining device (3) is connected with the fraction separating device (2), and the hydrofining discharging end (301) of the hydrofining device (3) is connected with the first fractionating device (4).
7. A system according to any one of claims 1 to 3, wherein the first fractionation device (4) comprises a first fractionation column (400), a first fractionation feed end (401) of the first fractionation column (400) being connected to the hydrofinishing device (3).
8. A system according to any one of claims 1 to 3, characterized in that the second fractionation unit (6) comprises a second fractionation column (600) with a second fractionation feed end (601) connected to the hydrocracking unit (5); the second fractionation discharging end (602) of the second fractionation tower (600) comprises a second rich gas discharging end (6021), a light naphtha discharging end (6022), a heavy naphtha discharging end (6023), an aviation kerosene discharging end (6024), a white oil discharging end (6025), a high cetane number diesel discharging end (6026) and a heavy component discharging end (6027).
9. A system according to claim 3, characterized in that the dewaxing unit (8) is provided with a dewaxing feed (800) and a dewaxing discharge (801), the dewaxing unit (8) comprising a third fractionation unit (9) connected to the dewaxing unit (8) for separating the catalytic reformate depleted of alkane components.
10. The system according to claim 9, characterized in that the third fractionation unit (9) comprises a third fractionation column (900), a third fractionation feed end (901) of the third fractionation column (900) being connected to a discharge end (801) of the dewaxing unit (8); the dewaxing discharge end (801) comprises an alkane discharge end (801 a) and a catalytic reforming product discharge end (801 b) for removing alkane components.
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| CN117844525A (en) * | 2024-03-07 | 2024-04-09 | 陕西煤业化工集团神木天元化工有限公司 | Method for preparing chemicals and special fuel from medium-temperature coal tar |
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