CN115466630A - Phenol tar hydrotreating method - Google Patents
Phenol tar hydrotreating method Download PDFInfo
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- CN115466630A CN115466630A CN202211104916.2A CN202211104916A CN115466630A CN 115466630 A CN115466630 A CN 115466630A CN 202211104916 A CN202211104916 A CN 202211104916A CN 115466630 A CN115466630 A CN 115466630A
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- fuel oil
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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000005336 cracking Methods 0.000 claims abstract description 33
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 20
- 239000000295 fuel oil Substances 0.000 claims abstract description 16
- 238000004821 distillation Methods 0.000 claims abstract description 10
- 239000002283 diesel fuel Substances 0.000 claims abstract description 8
- 239000010771 distillate fuel oil Substances 0.000 claims abstract description 8
- 239000010763 heavy fuel oil Substances 0.000 claims abstract description 8
- CJWNFAKWHDOUKL-UHFFFAOYSA-N 2-(2-phenylpropan-2-yl)phenol Chemical compound C=1C=CC=C(O)C=1C(C)(C)C1=CC=CC=C1 CJWNFAKWHDOUKL-UHFFFAOYSA-N 0.000 claims description 7
- 239000012043 crude product Substances 0.000 claims description 6
- 239000003921 oil Substances 0.000 claims description 3
- 239000011269 tar Substances 0.000 description 45
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- 238000000605 extraction Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 4
- KWOLFJPFCHCOCG-UHFFFAOYSA-N Acetophenone Chemical compound CC(=O)C1=CC=CC=C1 KWOLFJPFCHCOCG-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- XKZQKPRCPNGNFR-UHFFFAOYSA-N 2-(3-hydroxyphenyl)phenol Chemical compound OC1=CC=CC(C=2C(=CC=CC=2)O)=C1 XKZQKPRCPNGNFR-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical class [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005805 hydroxylation reaction Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- XDTRNDKYILNOAP-UHFFFAOYSA-N phenol;propan-2-one Chemical compound CC(C)=O.OC1=CC=CC=C1 XDTRNDKYILNOAP-UHFFFAOYSA-N 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
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
- C10G69/02—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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a phenol tar hydrotreating method, which comprises the following steps: firstly, feeding phenol tar into a light component separation tower to remove light components, and extracting heavy tar from a tower kettle; then the heavy tar is sent into a circulating reactor group to carry out two-stage high-temperature cracking reaction, and decomposed heavy components are extracted from the bottom of the circulating reactor group; then, the decomposed heavy components are sent to a hydrogenation reactor for hydrogenation reaction to obtain hydrogenated fuel oil; and finally, feeding the hydrogenated fuel oil into a primary distillation tower to separate the hydrogenated fuel oil, extracting light fuel oil from the tower top, extracting diesel oil from the side line, and extracting heavy fuel oil from the tower kettle. Compared with the prior art, the method adopts phenol and tar separation, hydrogenation is carried out after cracking, the resource utilization rate of tar is improved from 40-50% of cracking to 90-100%, and the green treatment of tar is realized.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and relates to a phenol tar hydrotreating method, in particular to a phenol tar hydrotreating method aiming at a byproduct of a process for producing phenol and bisphenol A by an isopropyl benzene method.
Background
Phenol tar is respectively from a phenol acetone device and a bisphenol A device. Wherein the phenol tar is a byproduct of a device for preparing phenol and acetone by using cumene as a raw material, is a distillation residue after phenol and acetone are separated as a reaction product, and belongs to hazardous waste. Phenol tar of bisphenol A apparatus is a tar of bisphenol A apparatus, and also contains phenol. At present, many phenol production plants can not effectively treat phenol tar, and basically adopt an incineration treatment method. By adopting the incineration treatment method, the recovered heat is limited, so that not only can the environmental pollution be caused, but also a large amount of carbon emission can be generated. Therefore, the method for directly recycling the tar by effectively reducing the discharge of the hazardous waste and by means of resource conversion has great value and environmental protection value.
Chinese patent CN 109647387 discloses a method for recovering diphenol by catalytic hydrocracking of phenol-containing tar and a catalyst. The method takes titanium dioxide modified by cesium salt loaded with palladium and silver as a catalyst, takes phenol-containing tar as a reaction raw material in an ethanol solvent, and directly catalyzes and hydrogenates the catalyst to directly synthesize the o/hydroquinone. According to the process, the phenol-containing tar is generated by hydroxylation reaction of phenol and hydrogen peroxide, the raw materials are different in composition source, and the recovered materials are different in purpose. And the patent mainly aims at the catalyst, and a specific process flow is not described.
Disclosure of Invention
The invention aims to provide a phenol tar hydrotreating method.
The purpose of the invention can be realized by the following technical scheme:
a phenol tar hydrotreating method comprises the following steps:
s1: sending the phenol tar into a light component separation tower to remove light components, and extracting heavy tar from a tower kettle;
s2: sending the heavy tar into a circulating reactor group to carry out two-stage high-temperature cracking reaction, wherein the bottom of the circulating reactor group is used for extracting decomposed heavy components; wherein, the circulating reactor group comprises a first cracking reactor and a second cracking reactor which are circularly connected;
s3: feeding the decomposed heavy components into a hydrogenation reactor to carry out hydrogenation reaction to obtain hydrogenated fuel oil;
s4: feeding the hydrogenated fuel oil into a primary distillation tower to separate the hydrogenated fuel oil, extracting light fuel oil from the tower top, extracting diesel oil from the side line, and extracting heavy fuel oil from the tower bottom.
Furthermore, the operation pressure at the top of the light component separation tower is 0.5-30 kPa, the temperature at the top of the tower is 80-180 ℃, the temperature at the bottom of the tower is 110-210 ℃, and the theoretical plate number is 50-120.
Furthermore, a cumylphenol crude product is extracted from the side line of the light component separation tower, and the extraction position is 10 th to 80 th theoretical plates.
Furthermore, a discharge port at the bottom of the circulating reactor group is also connected with a light component separation tower.
Further, the first cracking reactor is a plate tower reactor, the operating pressure at the top of the tower is gage pressure of 0.15-0.9 MPa, the temperature at the top of the tower is 150-280 ℃, the temperature at the bottom of the tower is 110-210 ℃, and the number of theoretical plates is 10-80;
the operating pressure of the second cracking reactor is 0.15-0.9 MPa of gauge pressure, the reaction temperature is 250-400 ℃, the feed inlet is connected with the tower kettle of the first cracking reactor, and the discharge outlet is connected with the feed inlet at the bottom of the first cracking reactor.
Further, the hydrogenation reactor is a fixed bed reactor.
Furthermore, in the hydrogenation reactor, the reaction pressure is 2.0-12.0 MPa gauge pressure, the reaction hydrogen-oil ratio is 200.
Furthermore, a feed inlet of the hydrogenation reactor is also connected with a light component separation tower kettle, and the ratio of the mass flow of the feed to the total mass flow of the heavy tar is 0.05-5.
Furthermore, an additional tar feeding hole is also formed in the hydrogenation reactor.
Furthermore, the operation pressure at the top of the primary distillation tower is 0.4-2 MPa of gauge pressure, the temperature at the top of the tower is 30-150 ℃, the temperature at the bottom of the tower is 150-280 ℃, and the number of theoretical plates is 20-90.
Compared with the prior art, the invention has the following characteristics:
1) Compared with the phenol tar cracking scheme, the method adopts phenol tar separation and hydrogenation after cracking. The resource utilization rate of tar is improved from 40-50% of cracking to 90-100%, and the green treatment of tar is realized;
2) The cracking reactor is also provided with a separation tower plate, so that light and heavy products can be separated in the reactor, heavy components are circularly reacted, and the retention time is prolonged. The light components can be extracted according to the product requirements;
3) After the light components are separated, the content of phenol in the material can be obviously reduced, and the consumption of hydrogen can be obviously reduced in the hydrogenation process.
4) The light cracking hydrogenation process combination adopted by the invention realizes the characteristic of wide raw material adaptability, and simultaneously, the light cracking hydrogenation process combination is treated with the non-phenol-containing tar of other devices in a combined way, thereby being particularly suitable for chemical integrated devices. By jointly treating the multi-device tar, the investment cost of repeated construction is reduced, and the operation cost of the hydrogenation process is reduced.
5) The hydrogen and heat energy required by the invention can be completely from renewable energy sources, and CO is basically avoided 2 Discharging and realizing green production of the device.
Drawings
FIG. 1 is a schematic structural diagram of a phenol tar hydrotreating process apparatus according to the present invention;
the notation in the figure is:
1-light component separation tower, 2-first cracking reactor, 3-second cracking reactor, 4-hydrogenation reactor and 5-preliminary distillation tower.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
A phenol tar hydrotreating method adopts a process unit as shown in figure 1 and comprises the following steps:
s1: sending phenol tar into a light component separation tower 1 for separation, collecting light components containing phenol from the top of the tower, collecting a cumylphenol crude product from the side line, and collecting heavy tar from the bottom of the tower;
wherein the operation pressure at the top of the light component separation tower 1 is 0.5-30 kPa absolute pressure, the temperature at the top of the tower is 80-180 ℃, the temperature at the bottom of the tower is 110-210 ℃, the reflux ratio is 3-10, the number of theoretical plates is 50-120, the feeding position of phenol tar is the first theoretical plate, and the lateral line extraction position is the 20 th-60 th theoretical plate; the purity of the obtained cumylphenol crude product is 30-80%;
when side draw is employed, the preferred overhead operating pressure is 1 to 8kPa (A), and the preferred column kettle temperature is 130 to 178 ℃;
s2: sending the heavy tar into a circulating reactor group to carry out two-stage high-temperature cracking reaction, wherein a decomposed light component product is produced at the top of the circulating reactor group, a decomposed heavy component is produced at the bottom of the circulating reactor group, the decomposed heavy component is divided into two strands, one strand of the heavy component is returned to a light component separation tower 1, and the other strand of the heavy component is sent into a hydrogenation reactor 4;
wherein, the circulating reactor group comprises a first cracking reactor 2 and a second cracking reactor 3 which are connected in a circulating way, and the circulating ratio is 1; preferably, the first cracking reactor 2 is internally provided with a separation tower plate for separating light components at the top of the tower, the operating pressure at the top of the tower is gage pressure of 0.15-0.9 MPa, the temperature at the top of the tower is 150-280 ℃, the temperature at the bottom of the tower is 110-210 ℃, and the number of theoretical tower plates is 10-80; the operating pressure of the second cracking reactor 3 is 0.15-0.9 MPa gauge pressure, the reaction temperature is 250-400 ℃, the feed inlet is connected with the tower kettle of the first cracking reactor 2, and the discharge outlet is connected with the bottom feed inlet of the first cracking reactor 2.
S3: the decomposed heavy components sent into the hydrogenation reactor 4 are saturated by hydrogenation to produce hydrogenated fuel oil;
wherein, the hydrogenation reactor 4 is a fixed bed reactor, hydrogen is introduced from the top of the reactor, the reaction pressure is gauge pressure of 2.0-12.0 MPa, the reaction hydrogen-oil ratio is 200;
preferably, the feed inlet of the hydrogenation reactor 4 is also connected with the tower kettle of the light component separation tower 1, namely, the heavy tar extracted from the tower kettle is used as a hydrogenation reaction raw material, and the ratio of the mass flow of the feed to the total mass flow of the heavy tar is 0.05-0.5; in addition, an additional tar inlet is also arranged on the hydrogenation reactor 4, and waste tar generated by other devices can be collected; namely, the reaction raw materials also comprise additional tar which does not contain phenol, such as coal tar or ethylene tar;
s4: feeding the hydrogenated fuel oil into a primary distillation tower 5 for separation, extracting light fuel oil rich in naphtha from the tower top, extracting diesel oil from the side line, and extracting heavy fuel oil from the tower bottom;
wherein the top operating pressure of the preliminary distillation tower 5 is 0.4-2 MPa gauge pressure, the top temperature is 30-150 ℃, the bottom temperature is 150-280 ℃, the reflux ratio is 2-8, the number of theoretical plates is 20-90, the feeding position of the hydrogenated fuel oil is 10-50 theoretical plates, and the lateral line discharging position is 6-45 theoretical plates; the mass flow rate ratio of the tower top extraction, the side extraction and the tower kettle extraction is as follows.
The present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
In the following examples; the phenol tar in examples 1-2 mainly consisted of: 12% of phenol, 14.3% of acetophenone and 73.7% of other components; the phenol tar in example 3 mainly consists of: 6.2 percent of phenol, 14.3 percent of acetophenone and 79.5 percent of other components.
Example 1:
a phenol tar hydrotreating method comprises the following steps:
s1: phenol tar is fed into a light component separation tower 1 at the flow rate of 100kg/h for separation, phenol-containing light components are extracted from the tower top at the flow rate of 26kg/h, and heavy tar is extracted from the tower bottom at the flow rate of 74kg/h;
wherein the tower top operating pressure of the light component separation tower 1 is 15kPa absolute pressure, and the purity of the obtained cumylphenol crude product is 47%;
s2: sending the heavy tar into a circulating reactor group to carry out two-stage high-temperature cracking reaction, wherein a decomposed light component product is extracted from the top of the circulating reactor group, the flow rate is 48kg/h, a decomposed heavy component is extracted from the bottom of the circulating reactor group, the decomposed heavy component is divided into two strands, one strand of the decomposed heavy component is returned to a light component separation tower 1, and the other strand of the decomposed heavy component is sent to a hydrogenation reactor 4;
s3: the decomposed heavy components sent into the hydrogenation reactor 4 are saturated by hydrogenation to produce hydrogenated fuel oil;
wherein the hydrogenation reactor 4 is a fixed bed reactor, hydrogen is introduced from the top of the reactor, the reaction pressure is gauge pressure of 3MPa, and the reaction temperature is 350 ℃;
s4: feeding the hydrogenated fuel oil into a primary distillation tower 5 at a flow rate of 55kg/h for separation, extracting light fuel oil rich in naphtha from the top of the tower, extracting diesel oil from the side of the tower, and extracting heavy fuel oil from the bottom of the tower;
wherein the operation pressure at the top of the primary tower 5 is 1MPa gauge pressure.
The mass flow ratio of the obtained light fuel oil, diesel oil and heavy fuel oil is 2.
Example 2:
a phenol tar hydrotreating process which differs from example 1 only in that:
in the step S1, the flow of the light component containing phenol extracted from the top of the light component separation tower 1 is 21kg/h; a crude cumylphenol product is extracted from the side of the light component separation tower 1, and the side extraction flow is 24kg/h; the purity of the obtained cumylphenol crude product is 55 percent;
in the step S2, the flow rate of the decomposed light component product extracted from the top of the circulating reactor group is 31kg/h;
in step S4, the flow rate of the hydrogenated fuel oil is 46kg/h, the mass flow rate ratio of the obtained light fuel oil, diesel oil and heavy fuel oil is 1.4.
Example 3:
compared with the embodiment 1, the method for hydrotreating the phenol tar only differs from the embodiment 1 in that:
in the step S1, the flow of the light component containing phenol extracted from the top of the light component separation tower 1 is 28kg/h;
in the step S2, the flow of the decomposed light component product extracted from the top of the circulating reactor group is 25kg/h;
in step S3, the reaction pressure is 6MPa gauge pressure,
in step S4, the flow rate of the hydrogenated fuel oil is 65kg/h, and the mass flow rate ratio of the obtained light fuel oil, diesel oil and heavy fuel oil is 2.3.
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (10)
1. A phenol tar hydrotreating method is characterized in that the method comprises the following steps:
s1: sending the phenol tar into a light component separation tower (1) to remove light components, and extracting heavy tar from a tower kettle;
s2: sending the heavy tar into a circulating reactor group to carry out two-stage high-temperature cracking reaction, wherein the bottom of the circulating reactor group is extracted to decompose heavy components; wherein the circulating reactor group comprises a first cracking reactor (2) and a second cracking reactor (3) which are connected in a circulating way;
s3: feeding the decomposed heavy components into a hydrogenation reactor (4) for hydrogenation reaction to obtain hydrogenated fuel oil;
s4: the hydrogenated fuel oil is sent into a primary distillation tower (5) to separate the hydrogenated fuel oil, light fuel oil is extracted from the top of the tower, diesel oil is extracted from the side of the tower, and heavy fuel oil is extracted from the bottom of the tower.
2. The phenol tar hydrotreating method according to claim 1, characterized in that the top operating pressure of the light component separation column (1) is 0.5 to 30kPa absolute, the top temperature is 80 to 180 ℃, the bottom temperature is 110 to 210 ℃, and the theoretical plate number is 50 to 120.
3. The phenol tar hydrotreating method according to claim 2, characterized in that the side line of the light component separation tower (1) is used for drawing a cumylphenol crude product, and the drawing position is 10-80 theoretical plates.
4. The phenol tar hydrotreating method according to claim 2, characterized in that the bottom discharge port of the circulating reactor group is further connected with a light component separation column (1).
5. The phenol tar hydrotreating method according to claim 1, characterized in that the first cracking reactor (2) is a plate column reactor, the operating pressure at the top of the column is 0.15-0.9 MPa gauge pressure, the temperature at the top of the column is 150-280 ℃, the temperature at the bottom of the column is 250-380 ℃, and the number of theoretical plates is 10-80;
the operating pressure of the second cracking reactor (3) is 0.15-0.9 MPa gauge pressure, the reaction temperature is 250-400 ℃, the feed inlet is connected with the tower kettle of the first cracking reactor (2), and the discharge outlet is connected with the bottom feed inlet of the first cracking reactor (2).
6. The method for hydrotreating phenol tar according to claim 1, characterized in that the hydrogenation reactor (4) is a fixed bed reactor.
7. The phenol tar hydrotreating method according to claim 1, characterized in that in the hydrogenation reactor (4), the reaction pressure is 2.0-12.0 MPa gauge, the reaction hydrogen-oil ratio is 200-1900.
8. The phenol tar hydrotreating method according to claim 1, characterized in that the feed inlet of the hydrogenation reactor (4) is further connected with the bottom of the light component separation tower (1), and the ratio of the feed mass flow to the total mass flow of the heavy tar is 0.05-5.
9. The phenol tar hydrotreating method according to claim 1, characterized in that the hydrogenation reactor (4) is further provided with an additional tar inlet.
10. The phenol tar hydrotreating method according to claim 1, characterized in that the operating pressure at the top of the preliminary distillation tower (5) is 0.4-2 MPa gauge pressure, the temperature at the top of the tower is 30-150 ℃, the temperature at the bottom of the tower is 150-280 ℃, and the number of theoretical plates is 20-90.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5457244A (en) * | 1994-10-04 | 1995-10-10 | General Electric Company | Phenol tar waste reduction process |
| EP0863195A1 (en) * | 1997-02-28 | 1998-09-09 | General Electric Company | Phenol tar cracking process |
| CN102633604A (en) * | 2012-04-20 | 2012-08-15 | 北京化工大学 | Method for recovering phenol and acetophenone from phenol tar |
| CN109647387A (en) * | 2018-12-26 | 2019-04-19 | 万华化学集团股份有限公司 | The method and catalyst of the cracking recycling diphenol of catalytic hydrogenation containing phenolic tar |
| CN111100658A (en) * | 2018-10-25 | 2020-05-05 | 榆林煤化工产业促进中心 | Coal chemical hydrogenation pyrolysis process |
-
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- 2022-09-09 CN CN202211104916.2A patent/CN115466630B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5457244A (en) * | 1994-10-04 | 1995-10-10 | General Electric Company | Phenol tar waste reduction process |
| CN1125250A (en) * | 1994-10-04 | 1996-06-26 | 通用电气公司 | Phenol tar waste reduction process |
| EP0863195A1 (en) * | 1997-02-28 | 1998-09-09 | General Electric Company | Phenol tar cracking process |
| CN102633604A (en) * | 2012-04-20 | 2012-08-15 | 北京化工大学 | Method for recovering phenol and acetophenone from phenol tar |
| CN111100658A (en) * | 2018-10-25 | 2020-05-05 | 榆林煤化工产业促进中心 | Coal chemical hydrogenation pyrolysis process |
| CN109647387A (en) * | 2018-12-26 | 2019-04-19 | 万华化学集团股份有限公司 | The method and catalyst of the cracking recycling diphenol of catalytic hydrogenation containing phenolic tar |
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