CN112939746A - Pre-pump mixing tower type continuous washing dephenolizing process - Google Patents
Pre-pump mixing tower type continuous washing dephenolizing process Download PDFInfo
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- CN112939746A CN112939746A CN202110153404.4A CN202110153404A CN112939746A CN 112939746 A CN112939746 A CN 112939746A CN 202110153404 A CN202110153404 A CN 202110153404A CN 112939746 A CN112939746 A CN 112939746A
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- pipeline
- separation
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- 238000005406 washing Methods 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000000926 separation method Methods 0.000 claims abstract description 116
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 claims abstract description 110
- 230000007935 neutral effect Effects 0.000 claims abstract description 52
- 239000003513 alkali Substances 0.000 claims abstract description 38
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 13
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 10
- 238000003780 insertion Methods 0.000 claims description 6
- 230000037431 insertion Effects 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 2
- 238000012423 maintenance Methods 0.000 abstract description 6
- 238000004939 coking Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- XTXZAZCDNWMPRK-UHFFFAOYSA-N naphthalene;phenol Chemical compound OC1=CC=CC=C1.C1=CC=CC2=CC=CC=C21 XTXZAZCDNWMPRK-UHFFFAOYSA-N 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/64—Preparation of O-metal compounds with O-metal group bound to a carbon atom belonging to a six-membered aromatic ring
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of metallurgical coking, in particular to a pre-pump mixing and tower type continuous washing dephenolizing process. 1) Mixing the unwashed mixed part and alkaline sodium phenolate in a pipeline mixer to generate a mixed part of neutral sodium phenolate and partial dephenolized sodium phenolate, and sending the mixed part into a separation tank; 2) carrying out standing separation, and then delivering neutral sodium phenolate; 3) the mixed part of the partial dephenolization is arranged at the upper part of the separation tank, and the mixed part of the partial dephenolization automatically flows to a continuous washing conveying pump from the upper part of the separation tank; 4) reacting phenol in the mixed part with partial dephenolization with alkali, and sending the reacted phenol and alkali into a continuous washing separation tower; 5) reacting alkali with the residual phenol in the mixed part to generate alkaline sodium phenolate and the mixed part, and standing and separating in a continuous washing separation tower; 6) the alkaline sodium phenolate automatically flows into the pipeline mixer to react with the unwashed mixed component and then is sent into the separation tank, and the mixed component is discharged from the top of the continuous washing separation tower through the washed mixed component pipeline. The process flow is simplified, the number of equipment is reduced, the investment and the occupied area are greatly reduced, and the operation and the maintenance are easier.
Description
Technical Field
The invention relates to the technical field of metallurgical coking, in particular to a pre-pump mixing and tower type continuous washing dephenolizing process.
Background
At present, in the metallurgical coking industry, the continuous washing and dephenolization mainly comprises the process of extracting phenol from phenol oil, naphthalene oil or phenol naphthalene washed and unwashed mixed parts cut by distillation of tar by using a 12% NaOH solution, for example, the unwashed mixed parts can react with alkali after being mixed with the 12% NaOH solution to generate water-soluble sodium phenolate, and the water-oil separation can be carried out on the phenol-removed mixed parts by standing.
The existing pre-pump mixing process flow is as follows: the unwashed mixed part and alkaline sodium phenolate from an alkaline sodium phenolate head tank are mixed before a mixed part conveying pump, the mixed part is stirred by the pump and then enters a primary continuous washing separation tower for standing oil-water separation, the bottom of the mixed part is used for obtaining neutral sodium phenolate of a dephenolized washed product, the mixed part after the top of the mixed part is washed by the primary dephenolizing buffer tank and 10% NaOH solution before the inlet of a secondary continuous washing pump, and the mixed part is stirred by the pump and then enters a secondary continuous washing separation tower for secondary dephenolizing washing. And obtaining alkaline sodium phenolate at the bottom of the tower, mixing the alkaline sodium phenolate with the unwashed mixed component before the alkaline sodium phenolate tank and the alkaline sodium phenolate head tank are conveyed to a mixed component conveying pump, obtaining the washed mixed component at the top of the tower, and conveying the mixed component to an industrial naphthalene distillation unit to be used as a raw material.
The existing process adopts a two-tower continuous washing dephenolization process, in order to meet the process requirements, equipment such as a buffer tank, a pump, a head tank and the like needs to be additionally arranged in the middle, the existing continuous washing dephenolization process has complex process flow, needs various equipment, greatly increases investment and occupied area, and has high production investment cost, inconvenient operation and maintenance and higher production and operation cost.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a mixing-before-pump tower type continuous washing dephenolizing process, which simplifies the process flow, reduces the number of equipment, greatly reduces the investment and the occupied area, and is easier to operate and overhaul.
In order to achieve the purpose, the invention adopts the following technical scheme:
a mixing-in-front pump tower type continuous washing dephenolizing system is provided, wherein continuous washing separation towers, separation tanks and neutral sodium phenolate tanks with different heights are respectively arranged from high to low according to the self-flowing direction of alkaline sodium phenolate and neutral sodium phenolate; the middle part of the separation tank is provided with an unwashed mixed part feeding distributor, and the tank is internally provided with an insertion pipe inserted into the bottom of the tank.
The bottom outlet of the continuous washing separation tower is connected with the inlet of the pipeline mixer through a pipeline, a liquid level regulator is arranged on the connected pipeline, the unwashed mixed part feeding pipeline is connected with the inlet of the pipeline mixer, the outlet of the pipeline mixer is connected with the top inlet of the separation tank, and a flow self-adjusting indicating instrument I is arranged on the unwashed mixed part feeding pipeline.
An outlet at the lower part of the neutral sodium phenolate groove is connected with a neutral sodium phenolate pipeline, and a neutral sodium phenolate delivery pump is arranged on the neutral sodium phenolate pipeline; an outlet at the upper part of the separation tank is connected with an inlet at the middle part of the continuous washing separation tower through a pipeline, a continuous washing delivery pump and a flow meter are arranged on the pipeline, the pipeline is connected with an outlet at the bottom of the alkali distribution tank through a branch pipeline, and an alkali pump and a flow self-regulation indicating meter II are arranged on the branch pipeline; the upper part of the continuous washing separation tower is connected with a washed mixed part pipeline.
A mixing-tower-type continuous washing dephenolizing process before pumping specifically comprises the following steps:
1) conveying the unwashed mixed part to a pipeline mixer through an unwashed mixed part feeding pipeline, controlling the adding amount of the unwashed mixed part through a flow self-regulation indicating instrument I, conveying the alkaline sodium phenolate to the pipeline mixer from the bottom of a continuous washing separation tower, mixing the unwashed mixed part and the alkaline sodium phenolate in the pipeline mixer, reacting free alkali in the alkaline sodium phenolate with a phenol part in the mixed part to generate a mixed part of neutral sodium phenolate and part of dephenolized mixed part, conveying the mixed part to the middle position in a separation tank together, and uniformly distributing the mixed part to the middle of the separation tank through a distributor in the separation tank;
2) the mixed part of the partial dephenolization and the neutral sodium phenolate are subjected to standing separation, the density of the neutral sodium phenolate is higher at the lower part of the separation tank according to the different density difference of the mixed part and the neutral sodium phenolate, the neutral sodium phenolate fully flows into a neutral sodium phenolate tank lower than the separation tank through an insertion pipe in the tank, and then the neutral sodium phenolate is conveyed to the next unit through a neutral sodium phenolate pipeline by a neutral sodium phenolate conveying pump;
3) the density of the mixed part of the partial dephenolization is light at the upper part of the separation tank, and the mixed part of the partial dephenolization automatically flows to a continuous washing conveying pump from the upper part of the separation tank;
4) the prepared NaOH solution with the concentration of 12% is stored in an alkali preparation tank and then is conveyed to a continuous washing conveying pump through an alkali pump, the addition amount of the alkali solution is controlled through a flow self-regulation indicating instrument II, phenol and alkali in the mixed part with partial dephenolization are fully mixed and reacted through the continuous washing conveying pump and then are conveyed to the middle part of a continuous washing separation tower, and the flow of the mixed solution is checked through a flow instrument;
5) alkali reacts with the residual phenol in the mixed part to generate alkaline sodium phenolate and the mixed part, the alkaline sodium phenolate and the mixed part are kept stand and separated in a continuous washing separation tower, the density of the alkaline sodium phenolate is higher than that of the lower part of the continuous washing separation tower, the density of the mixed part is lower than that of the upper part of the continuous washing separation tower, and the interface of the alkaline sodium phenolate and the mixed part is controlled by adjusting the liquid level height of an alkaline sodium phenolate outlet through a liquid level regulator;
6) the alkaline sodium phenolate automatically flows to a pipeline mixer to be fully mixed and reacted with the unwashed mixed component pumped by a pump, and then the alkaline sodium phenolate is sent into a separation tank, and the mixed component is discharged from the top of a continuous washing separation tower through a washed mixed component pipeline and is sent to an industrial naphthalene distillation unit as a raw material.
Compared with the prior art, the invention has the beneficial effects that:
1) the invention is provided with a separation tank for primary separation, the unwashed mixed part pumped by a pump and the alkaline sodium phenolate from the bottom of the continuous washing tower are mixed by a pipeline mixer and then are sent to the middle part of the separation tank, a distributor is arranged in the middle part of the separation tank to uniformly distribute the incoming mixed material again, and the separation tank is kept still for separation.
2) Compared with the traditional process, the pipeline mixer is added, and an alkaline sodium phenolate tank, an alkaline sodium phenolate pump and an alkaline sodium phenolate head tank are reduced. The alkaline sodium phenolate from the bottom of the continuous washing separation tower enters the pipeline mixer after passing through the liquid level regulator, and the unwashed mixed component pumped by the external pump and the alkaline sodium phenolate are fully mixed and reacted at the pipeline mixer and then are sent to the middle part in the separation tank, so that the process flow is simpler.
3) Compared with the traditional process, the process has the advantages of adding the separation tank, reducing the number of the primary continuous washing separation tower, the primary dephenolization buffer tank, the liquid level regulator and the process equipment, along with simple operation and easy operation and maintenance.
4) In the process flow of the invention, a plurality of media completely flow by self-flow, so that the height difference of equipment can be well set, a plurality of intermediate equipment is reduced, compared with the traditional process, the process equipment is less, and the investment and the occupied area are greatly reduced.
5) Compared with the traditional process, the process flow is simpler, and the operation and maintenance are easy.
Drawings
FIG. 1 is a schematic diagram of the structure and process of the present invention.
In the figure: 1-separation tank 2-continuous washing delivery pump 3-continuous washing separation tower 4-alkali preparation tank 5-alkali pump 6-liquid level regulator 7-pipeline mixer 8-washed mixed component pipeline 9-flow self-regulation indicator instrument I10-flow self-regulation indicator instrument II 11-neutral sodium phenolate tank 12-neutral sodium phenolate delivery pump 13-distributor 14-insert pipe 15-flow instrument
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in figure 1, a pre-pump mixing and tower type continuous washing dephenolizing system is provided with a continuous washing separation tower 3, a separation tank 1 and a neutral sodium phenolate tank 11 which are arranged at different heights from right to left and from high to low according to the self-flowing direction of alkaline sodium phenolate and neutral sodium phenolate. Continuous washing separation tower 3: DN 2000mm H18000 mm VN 25m 3; separation tank 1: DN 4400mm H6965 mm VN 90m 3; neutral sodium phenolate tank 11: DN 4400mm H4205 mm VN 50m 3.
The outlet at the lower part of the neutral sodium phenolate tank 11 is connected with a neutral sodium phenolate pipeline, and a neutral sodium phenolate delivery pump 12 is arranged on the neutral sodium phenolate pipeline. An outlet at the upper part of the separation tank 1 is connected with an inlet at the top of the neutral sodium phenolate tank 11 through a pipeline.
The middle part of the separation tank 1 is provided with an unwashed mixed part feeding distributor 13, a neutral sodium phenolate outlet is connected out from the upper part of the separation tank, an insertion pipe 14 inserted into the bottom of the separation tank is arranged in the separation tank, and a mixed part outlet is arranged at the upper part of the separation tank.
The outlet at the bottom of the continuous washing separation tower 3 is connected with the inlet of a pipeline mixer 7 through a pipeline, a liquid level regulator 6 is arranged on the connected pipeline, the unwashed mixed part feeding pipeline is connected with the inlet of the pipeline mixer 7, the outlet 7 of the pipeline mixer is connected with the inlet at the top of the separation tank 1, and a flow self-regulation indicating instrument I9 is arranged on the unwashed mixed part feeding pipeline.
The upper outlet of the separating tank 1 is connected with the middle inlet of the continuous washing separating tower 3 through a pipeline, the pipeline is provided with a continuous washing delivery pump 2 and a flow meter 15, the pipeline is connected with the bottom outlet of the alkali distributing tank 4 through a branch pipeline, and the branch pipeline is provided with an alkali pump 5 and a flow self-regulating indicator meter two 10. The upper part of the continuous washing separation tower 3 is connected with a washed mixed part pipeline 8.
A mixing-tower-type continuous washing dephenolizing process before a pump specifically comprises the following steps:
1) the pumped unwashed mixed part is conveyed to a pipeline mixer 7 through an unwashed mixed part feeding pipeline, the adding amount of the unwashed mixed part is controlled by a first flow self-regulation indicating instrument 9, alkaline sodium phenolate is conveyed to the pipeline mixer 7 from the bottom of a continuous washing separation tower 3, the unwashed mixed part and the alkaline sodium phenolate are mixed in the pipeline mixer 7, free alkali in the alkaline sodium phenolate reacts with a phenol part in the mixed part to generate neutral sodium phenolate and the mixed part with partial dephenolization which are conveyed to the middle position in a separation tank 1 together, and then the neutral sodium phenolate and the mixed part are uniformly distributed in the middle of the separation tank 1 through a distributor 13 in the separation tank 1.
2) The mixed part of the partial dephenolization and the neutral sodium phenolate are kept stand and separated, the density of the neutral sodium phenolate is higher at the lower part of the separation tank 1 according to the different density difference of the two, the neutral sodium phenolate flows into a neutral sodium phenolate tank 11 which is lower than the separation tank 1 through an insertion pipe 14 in the tank, and then the neutral sodium phenolate is conveyed to the next unit by a neutral sodium phenolate conveying pump 12.
3) The density of the mixed part of the partial dephenolization is light at the upper part of the separation tank 1, and the mixed part of the partial dephenolization automatically flows to the continuous washing conveying pump 2 from the upper part of the separation tank 1.
4) And the prepared NaOH solution with the concentration of 12% is stored in an alkali preparation tank 4 and then is conveyed to the continuous washing conveying pump 2 through an alkali pump 5, the addition amount of the alkali solution is controlled through a flow self-regulation indicating instrument II 10, phenol and alkali in the mixed part with partial dephenolization are fully mixed and reacted through the continuous washing conveying pump 2 and then are conveyed to the middle part of the continuous washing separation tower 3, and the flow of the mixed solution is checked through a flow instrument 15.
5) Alkali reacts with the residual phenol in the mixed part, alkaline sodium phenolate and the mixed part are generated due to excessive alkali, standing separation is carried out in the continuous washing separation tower 3 according to different density differences of the alkaline sodium phenolate and the mixed part, the density of the alkaline sodium phenolate is higher than that of the lower part of the continuous washing separation tower 3, the density of the mixed part is lighter than that of the upper part of the continuous washing separation tower 3, and in order to control the feeding position, the alkaline sodium phenolate is preferably arranged at the middle feeding position of the continuous washing separation tower, and the alkaline sodium phenolate needs to be adjusted by a liquid level adjuster 6 to adjust the liquid level height of an alkaline.
6) Because the continuous washing separation tower 3 is higher, the height of the alkaline sodium phenolate from the liquid level regulator 6 is far higher than the top of the separation tank 1, and the alkaline sodium phenolate automatically flows to the pipeline mixer 7 to be fully mixed and reacted with the unwashed mixed component pumped by the pump, and then is sent into the separation tank 1. The mixed part is discharged from a washed mixing pipe 8 at the top of the continuous washing separation tower 3 and is sent to an industrial naphthalene distillation unit as a raw material.
7) The flow of the main materials is provided with a plurality of necessary instruments, the adding amount of the unwashed mixed components and the alkali which are pumped is controlled by a first flow self-regulating indicating instrument 9 and a second flow self-regulating indicating instrument 10, and the flow is indicated and checked by a flow instrument 15 after the conveying pump is continuously washed. Other positions can be provided with corresponding meters according to the requirements of different users.
The invention is provided with a separation tank 1 for primary separation, the unwashed mixed part pumped by a pump is mixed with alkaline sodium phenolate from the bottom of a continuous washing separation tower 3 through a pipeline mixer 7 and then is sent to the middle part of the separation tank 1, a distributor 13 is arranged in the middle part of the separation tank 1, the incoming mixed material is uniformly distributed again, and the separation tank is kept still for separation, because the volume of the separation tank 1 is far larger than that of the continuous washing separation tower 3, the retention time is increased, and the separation effect is better.
Compared with the traditional process, the pipeline mixer 7 is added, and an alkaline sodium phenolate tank, an alkaline sodium phenolate pump and an alkaline sodium phenolate head tank are reduced. The alkaline sodium phenolate from the bottom of the continuous washing separation tower 3 enters a pipeline mixer 7 after passing through a liquid level regulator 6, and the unwashed mixed part pumped from the outside and the alkaline sodium phenolate are fully mixed and reacted at the pipeline mixer 7 and then are sent to the middle part in the separation tank 1, so that the process flow is simpler.
Compared with the traditional process, the separation tank 1 is added, the number of the continuous washing separation tower, the dephenolization buffer tank and the liquid level regulator is reduced, the process equipment is less, the operation is simple, and the operation and the maintenance are easy. In the process flow of the invention, a plurality of media completely flow by self-flow, so that the height difference of equipment can be well set, a plurality of intermediate equipment is reduced, compared with the traditional process, the process equipment is less, and the investment and the occupied area are greatly reduced. Compared with the traditional process, the process flow is simpler, and the operation and maintenance are easy.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (5)
1. A mixed tower type continuous washing dephenolizing process before a pump, wherein a system is provided with continuous washing separation towers, separation tanks and neutral sodium phenolate tanks with different heights from high to low respectively according to the self-flowing direction of alkaline sodium phenolate and neutral sodium phenolate; the middle part of the separation tank is provided with an unwashed mixed part feeding distributor, and the tank is internally provided with an insertion pipe inserted into the bottom of the tank;
an outlet at the bottom of the continuous washing separation tower is connected with an inlet of a pipeline mixer through a pipeline, a liquid level regulator is arranged on the connected pipeline, an unwashed mixed part feeding pipeline is connected with an inlet of the pipeline mixer, an outlet of the pipeline mixer is connected with an inlet at the top of the separation tank, and a first flow self-regulating indicating instrument is arranged on the unwashed mixed part feeding pipeline;
an outlet at the lower part of the neutral sodium phenolate groove is connected with a neutral sodium phenolate pipeline, and a neutral sodium phenolate delivery pump is arranged on the neutral sodium phenolate pipeline; an outlet at the upper part of the separation tank is connected with an inlet at the middle part of the continuous washing separation tower through a pipeline, a continuous washing delivery pump and a flow meter are arranged on the pipeline, the pipeline is connected with an outlet at the bottom of the alkali distribution tank through a branch pipeline, and an alkali pump and a flow self-regulation indicating meter II are arranged on the branch pipeline; the upper part of the continuous washing separation tower is connected with a washed mixed part pipeline;
the method is characterized by comprising the following steps:
1) conveying the unwashed mixed part to a pipeline mixer through an unwashed mixed part feeding pipeline, conveying the alkaline sodium phenolate to the pipeline mixer from the bottom of a continuous washing separation tower, mixing the unwashed mixed part and the alkaline sodium phenolate in the pipeline mixer, reacting free alkali in the alkaline sodium phenolate with a phenol part in the mixed part to generate a neutral sodium phenolate and a mixed part with partial dephenolization, conveying the neutral sodium phenolate and the mixed part with partial dephenolization to the middle position in a separation tank, and uniformly distributing the neutral sodium phenolate and the mixed part in the separation tank through a distributor in the separation tank;
2) the mixed part of the partial dephenolization and the neutral sodium phenolate are subjected to standing separation, the density of the neutral sodium phenolate is higher at the lower part of the separation tank according to the different density difference of the mixed part and the neutral sodium phenolate, the neutral sodium phenolate fully flows into a neutral sodium phenolate tank lower than the separation tank through an insertion pipe in the tank, and then the neutral sodium phenolate is conveyed to the next unit through a neutral sodium phenolate pipeline by a neutral sodium phenolate conveying pump;
3) the density of the mixed part of the partial dephenolization is light at the upper part of the separation tank, and the mixed part of the partial dephenolization automatically flows to a continuous washing conveying pump from the upper part of the separation tank;
4) the prepared alkali solution with the concentration is stored in an alkali preparation tank and then is conveyed to a continuous washing conveying pump through an alkali pump, and phenol and alkali in the partially dephenolized mixed part are fully mixed and reacted through the continuous washing conveying pump and then are conveyed to the middle part of a continuous washing separation tower;
5) alkali reacts with the residual phenol in the mixed part to generate alkaline sodium phenolate and the mixed part, the alkaline sodium phenolate and the mixed part are kept stand and separated in a continuous washing separation tower, the density of the alkaline sodium phenolate is higher than that of the lower part of the continuous washing separation tower, the density of the mixed part is lower than that of the upper part of the continuous washing separation tower, and the interface of the alkaline sodium phenolate and the mixed part is controlled by adjusting the liquid level height of an alkaline sodium phenolate outlet through a liquid level regulator;
6) the alkaline sodium phenolate automatically flows to a pipeline mixer to be fully mixed and reacted with the unwashed mixed component pumped by a pump, and then the alkaline sodium phenolate is sent into a separation tank, and the mixed component is discharged from the top of a continuous washing separation tower through a washed mixed component pipeline and is sent to an industrial naphthalene distillation unit as a raw material.
2. The pre-pump mixing-tower continuous washing dephenolation process as claimed in claim 1, wherein the prepared alkali solution of step 4) is a 12% NaOH solution.
3. The pre-pump mixing-tower type continuous washing dephenolation process as claimed in claim 1, wherein the unwashed mixed portion in step 1) is delivered to the pipeline mixer through an unwashed mixed portion feeding pipeline, and the amount of the unwashed mixed portion is controlled by a flow self-regulation indicator instrument.
4. The pre-pump mixing-tower type continuous washing and dephenolizing process as claimed in claim 1, wherein the prepared alkali solution with the prepared concentration in step 4) is stored in an alkali preparation tank and then is delivered to a continuous washing delivery pump through an alkali pump, and the addition amount of the alkali solution is controlled through a flow self-regulation indicator instrument II.
5. The pre-pump mixing and tower type continuous washing dephenolization process as claimed in claim 1, wherein phenol and alkali in the mixed part of the partial dephenolization in the step 4) are fully mixed and reacted by a continuous washing delivery pump and then are sent to the middle part of the continuous washing separation tower, and the flow of the mixed solution is checked through a flow meter.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475817A (en) * | 2008-12-18 | 2009-07-08 | 中冶焦耐工程技术有限公司 | Distillate dephenolizing process and apparatus thereof |
| CN102381943A (en) * | 2011-08-30 | 2012-03-21 | 河南宝舜化工科技有限公司 | System and technology for producing coked crude phenol |
| CN202265523U (en) * | 2011-08-30 | 2012-06-06 | 河南宝舜化工科技有限公司 | Production system for coking crude phenol |
| CN102964220A (en) * | 2012-11-28 | 2013-03-13 | 中冶焦耐工程技术有限公司 | Pure sodium phenolate sulfuric acid continuous decomposition technology and equipment thereof |
| CN205528524U (en) * | 2016-01-21 | 2016-08-31 | 陕西华祥能源科技集团有限公司 | Utilize phenol sodium salt to prepare device of crude carbolic acid |
| CN109647005A (en) * | 2019-01-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | Hybrid technique and device before a kind of dephenolize washing pump |
| CN109651092A (en) * | 2019-01-24 | 2019-04-19 | 山西永东化工股份有限公司 | A kind of gas circulation coking crude phenol clean preparation method and its device |
| CN109762592A (en) * | 2019-03-11 | 2019-05-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of pair of spray formula and the joint dephenolize washing process and system for pumping front mixing combination |
| CN209778756U (en) * | 2019-03-11 | 2019-12-13 | 中冶焦耐(大连)工程技术有限公司 | combined dephenolizing washing system combining opposite spraying and pre-pump mixing |
| CN209985425U (en) * | 2019-04-25 | 2020-01-24 | 中冶焦耐(大连)工程技术有限公司 | Efficient continuous washing separation tower |
| CN111689837A (en) * | 2020-06-10 | 2020-09-22 | 山西永东化工股份有限公司 | Coking crude phenol production method and production device capable of effectively reducing discharge of three wastes |
-
2021
- 2021-02-04 CN CN202110153404.4A patent/CN112939746A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475817A (en) * | 2008-12-18 | 2009-07-08 | 中冶焦耐工程技术有限公司 | Distillate dephenolizing process and apparatus thereof |
| CN102381943A (en) * | 2011-08-30 | 2012-03-21 | 河南宝舜化工科技有限公司 | System and technology for producing coked crude phenol |
| CN202265523U (en) * | 2011-08-30 | 2012-06-06 | 河南宝舜化工科技有限公司 | Production system for coking crude phenol |
| CN102964220A (en) * | 2012-11-28 | 2013-03-13 | 中冶焦耐工程技术有限公司 | Pure sodium phenolate sulfuric acid continuous decomposition technology and equipment thereof |
| CN205528524U (en) * | 2016-01-21 | 2016-08-31 | 陕西华祥能源科技集团有限公司 | Utilize phenol sodium salt to prepare device of crude carbolic acid |
| CN109647005A (en) * | 2019-01-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | Hybrid technique and device before a kind of dephenolize washing pump |
| CN109651092A (en) * | 2019-01-24 | 2019-04-19 | 山西永东化工股份有限公司 | A kind of gas circulation coking crude phenol clean preparation method and its device |
| CN109762592A (en) * | 2019-03-11 | 2019-05-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of pair of spray formula and the joint dephenolize washing process and system for pumping front mixing combination |
| CN209778756U (en) * | 2019-03-11 | 2019-12-13 | 中冶焦耐(大连)工程技术有限公司 | combined dephenolizing washing system combining opposite spraying and pre-pump mixing |
| CN209985425U (en) * | 2019-04-25 | 2020-01-24 | 中冶焦耐(大连)工程技术有限公司 | Efficient continuous washing separation tower |
| CN111689837A (en) * | 2020-06-10 | 2020-09-22 | 山西永东化工股份有限公司 | Coking crude phenol production method and production device capable of effectively reducing discharge of three wastes |
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Application publication date: 20210611 |