CN112521253A - Carbon dioxide decomposition system and process for sodium phenolate - Google Patents
Carbon dioxide decomposition system and process for sodium phenolate Download PDFInfo
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- CN112521253A CN112521253A CN202011505439.1A CN202011505439A CN112521253A CN 112521253 A CN112521253 A CN 112521253A CN 202011505439 A CN202011505439 A CN 202011505439A CN 112521253 A CN112521253 A CN 112521253A
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- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 162
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 72
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 title claims abstract description 51
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 36
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 34
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 191
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 118
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 98
- 238000000926 separation method Methods 0.000 claims abstract description 64
- 230000020477 pH reduction Effects 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 239000003546 flue gas Substances 0.000 claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229940031826 phenolate Drugs 0.000 claims abstract description 15
- ISWSIDIOOBJBQZ-UHFFFAOYSA-M phenolate Chemical compound [O-]C1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-M 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 239000007789 gas Substances 0.000 claims description 32
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 239000007864 aqueous solution Substances 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 15
- 239000007795 chemical reaction product Substances 0.000 claims description 12
- 238000012856 packing Methods 0.000 claims description 11
- 230000005484 gravity Effects 0.000 claims description 9
- 239000000945 filler Substances 0.000 claims description 7
- 230000005587 bubbling Effects 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 2
- 238000004821 distillation Methods 0.000 abstract description 3
- 238000004939 coking Methods 0.000 abstract description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 8
- 238000000746 purification Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- PYOZTOXFQNWBIS-UHFFFAOYSA-N phenol;sodium Chemical class [Na].OC1=CC=CC=C1 PYOZTOXFQNWBIS-UHFFFAOYSA-N 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 235000011152 sodium sulphate Nutrition 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000004707 phenolate Chemical group 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000002351 wastewater Substances 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
- C07C37/01—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by replacing functional groups bound to a six-membered aromatic ring by hydroxy groups, e.g. by hydrolysis
- C07C37/055—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by replacing functional groups bound to a six-membered aromatic ring by hydroxy groups, e.g. by hydrolysis the substituted group being bound to oxygen, e.g. ether group
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
-
- 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
- C07C37/005—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by obtaining phenols from products, waste products or side-products of processes, not directed to the production of phenols, by conversion or working-up
- C07C37/007—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by obtaining phenols from products, waste products or side-products of processes, not directed to the production of phenols, by conversion or working-up from the tar industry
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/80—Organic bases or salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
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Abstract
The invention relates to equipment and a process of a tar distillation phenate decomposition unit in the coking industry, in particular to a system and a process for decomposing carbon dioxide of sodium phenolate. The device comprises a decomposition tower, a crude phenol acidification tower, a sodium carbonate treatment tower and a primary decomposition separation tank, wherein the decomposition tower is divided into an upper section, a middle section and a lower section; the flue gas pipeline is respectively connected with the middle section of the decomposition tower, the lower section of the decomposition tower, the upper section of the crude phenol acidification tower and the upper section of the sodium carbonate treatment tower, the upper section of the crude phenol acidification tower is connected with the middle section of the decomposition tower through a pipeline, and the upper section of the sodium carbonate treatment tower is connected with the middle section of the decomposition tower through a pipeline; the decomposition tower, the crude phenol acidification tower and the sodium carbonate treatment tower are respectively connected with the primary decomposition separation tank through pipelines. Three towers are used for replacing six towers in the original process, three delivery pumps and three liquid level recording and adjusting instruments are reduced, so that a large amount of operation cost is saved, the occupied area is reduced, and the phenolate decomposition rate and the intrinsic safety of the whole process are improved.
Description
Technical Field
The invention relates to equipment and a process of a tar distillation phenate decomposition unit in the coking industry, in particular to a system and a process for decomposing carbon dioxide of sodium phenolate.
Background
The coal tar contains various organic matters, wherein phenols account for 1-2% and are relatively expensive components, phenol sodium salts are obtained by fraction washing mainly in a three-mixed fraction (phenol oil, naphthalene oil and wash oil) obtained after distillation of the coal tar, namely after the three-mixed fraction is mixed with a 12% NaOH solution, phenols in the mixed fraction react with alkali to generate water-soluble phenol sodium salts, the water-soluble phenol sodium salts can be obtained by standing and oil-water separation of the phenol sodium salts and the dephenolized mixed fraction, and crude phenol is obtained by phenolate decomposition, namely acidolysis.
The decomposition of phenate is generally carried out by a sulfuric acid method and a carbon dioxide decomposition method, wherein the sulfuric acid decomposition method is divided into a batch decomposition and a continuous decomposition.
The main equipment of the batch sulfuric acid decomposition method is a batch decomposer; the sodium phenolate was charged into the decomposer neat, and then sulfuric acid was slowly charged from an overhead tank, and about 75% sulfuric acid was generally injected while stirring. The heat generated in the decomposition process is removed by indirect cooling water. Standing for several hours after reaction, floating the coarse powder generated by decomposition on the upper surface and precipitating sodium sulfate on the lower surface, so that waste water containing sodium sulfate is firstly discharged, and then the crude phenol is discharged.
A process for continuously decomposing sodium phenolate with sulfuric acid includes such steps as continuously mixing clean sodium phenolate solution with sulfuric acid by spraying mixer, passing through pipeline mixer and phenolate decomposing heater, and separating to obtain crude phenol and sodium sulfate.
The sulfuric acid method basically belongs to a elimination process, and a carbon dioxide decomposition method is mainly adopted at present.
The carbon dioxide decomposition method is to use flue gas or blast furnace gas to decompose sodium phenolate by using carbon dioxide component contained in the flue gas, i.e. sodium phenolate and carbon dioxide are reacted in aqueous solution to produce crude phenol and sodium carbonate, when the carbon dioxide is excessive, the reaction produces sodium bicarbonate, if sodium bicarbonate is found in the sodium carbonate solution, the decomposition is complete.
As shown in FIG. 1, the basic flow of the carbon dioxide decomposition method is as follows:
the carbon dioxide-containing flue gas sent from the outside of the device is boosted by a flue gas fan (10) and then sent to a No. 1 decomposition tower (2), a No. 2 decomposition tower (3), a crude phenol acidification tower (4) and a sodium carbonate treatment tower (5) for decomposing sodium phenolate in a liquid phase; the clean sodium phenolate in the clean sodium phenolate tank is pumped into a tail gas washing tower (1), tail gas after decomposition of phenolate introduced from the bottom is sprayed and washed from the top and is in countercurrent contact with the tail gas introduced from the bottom in a packing layer, and a small amount of phenol brought out when the phenolate decomposition of flue gas is carried out in the tail gas is neutralized by using alkali remained in the clean sodium phenolate tank in the washing process, so that the tail gas is washed; then the mixture is sent into a 1# decomposition tower (2) through a sodium phenolate pump (11), the liquid level LRC-01 of the tail gas holding washing tower (1) is adjusted by a liquid adjusting valve I to stably control the flow of the sodium phenolate, the sodium phenolate is in parallel-current contact with carbon dioxide gas entering from the bottom in the 1# decomposition tower (2) to carry out bubbling mass transfer, a chemical reaction is carried out, and phenolic substances and sodium carbonate are generated; the reaction product flows from the middle section of the column to the No. 2 decomposition column (3), and the decomposition reaction is continued with the carbon dioxide blown in from the bottom of the column, and the above process is called primary decomposition.
The reaction product flowing out from the middle section of the 2# decomposition tower (3) is discharged into a primary decomposition separation tank (7) for oil-water separation, primary decomposed phenol floats on the liquid surface and flows to the other side through an internal partition plate, the separated primary decomposed phenol is sent into a crude phenol acidification tower (4) through a primary decomposed phenol pump (12), and the primary decomposed phenol and carbon dioxide blown in from the bottom of the tower are subjected to decomposition reaction in the tower, wherein the process is called secondary decomposition and is also a decomposition and purification process of residual sodium phenolate in the crude phenol.
The reaction product is discharged from the full flow port at the middle section of the crude phenol acidification tower (4), flows into a secondary decomposition separation tank (8), wherein the secondary decomposition phenol and the sodium carbonate aqueous solution are separated, and the secondary decomposition phenol is pressurized by a secondary decomposition phenol pump (13) and then is sent out.
The sodium carbonate aqueous solution separated by the primary decomposition separation tank (7) and the secondary decomposition separation tank (8) is discharged into a sodium carbonate working tank (9) together in a full flow mode, the sodium carbonate aqueous solution is sent to the top of a sodium carbonate treatment tower (5) by a sodium carbonate working pump (14) to be sprayed, and is in countercurrent contact with the flue gas introduced from the bottom at a packing layer to be used for decomposing residual sodium phenolate in the sodium carbonate solution, the reacted reactant is sent to a sodium carbonate oil-water separation tower (6) by a sodium carbonate pump (15) to be subjected to oil-water separation, the crude phenol amount of the full flow at the top is little, the primary decomposition separation tank (7) is sent back, and the pure sodium carbonate full.
The existing carbon dioxide decomposition process has multiple devices and single function, all the devices are conveyed by virtue of conveying pumps, each conveying pump is additionally provided with a liquid level recording and adjusting instrument which is provided with a liquid level adjusting valve I (16), a liquid level adjusting valve II (17), a liquid level adjusting valve III (18) and a liquid level adjusting valve IV (19), the control is complicated, the occupied area is large, the operation cost is high, a plurality of factors which can be optimized and integrated are needed to be improved, and the use area and the operation cost are saved.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a system and a process for decomposing sodium phenolate by carbon dioxide, wherein one decomposition tower is adopted to complete the cleaning of tail gas and the primary decomposition of sodium phenolate, an improved crude phenol acidification tower with a filler is adopted to complete the secondary decomposition and oil-water separation of primary decomposed phenol, the decomposition rate of phenolate is improved, an improved sodium carbonate treatment tower is adopted to treat the purification and oil-water separation of sodium carbonate, three towers are used for replacing six towers in the original flow, three delivery pumps and three liquid level recording and adjusting instruments are reduced, so that a large amount of operation cost is saved, the occupied area is reduced, and the phenolate decomposition rate and the intrinsic safety of the whole process are improved.
In order to achieve the purpose, the invention adopts the following technical scheme:
the carbon dioxide decomposition system of sodium phenolate comprises a decomposition tower, a crude phenol acidification tower, a sodium carbonate treatment tower and a primary decomposition separation tank, wherein the decomposition tower is divided into an upper section, a middle section and a lower section; the flue gas pipeline is respectively connected with the middle section of the decomposition tower, the lower section of the decomposition tower, the upper section of the crude phenol acidification tower and the upper section of the sodium carbonate treatment tower through branch pipelines, the upper section of the crude phenol acidification tower is connected with the middle section of the decomposition tower through a pipeline, and the upper section of the sodium carbonate treatment tower is connected with the middle section of the decomposition tower through a pipeline; the decomposition tower, the crude phenol acidification tower and the sodium carbonate treatment tower are respectively connected with the primary decomposition separation tank through pipelines. And a flue gas fan is arranged on the flue gas pipeline.
And a pipeline connecting the primary decomposition separation tank and the crude phenol acidification tower is provided with a primary decomposition phenol pump and a liquid level regulating valve.
The decomposing tower is divided into an upper section, a middle section and a lower section, the top is a tail gas washing section, the middle is a 1# decomposing section, the bottom is a 2# decomposing section, the crude phenol acidifying tower is divided into an upper section and a lower section, the upper section is a crude phenol acidifying section, a filler is arranged in the upper section, and the lower section is an oil-water separation section.
The sodium carbonate treatment tower is divided into an upper section and a lower section, the upper section is a sodium carbonate treatment section, and the lower section is an oil-water separation section.
A carbon dioxide decomposition process of sodium phenolate specifically comprises the following steps:
1) the flue gas containing carbon dioxide is pressurized by a flue gas fan and then sent into the middle section and the lower section of a decomposing tower, the upper section of a crude phenol acidification tower and the upper section of a sodium carbonate treatment tower,
2) primary decomposition:
the clean sodium phenolate is sent into the decomposing tower from the upper section of the decomposing tower, tail gas after phenolate decomposition of the middle section and the lower section which are introduced from the top and washed from the bottom, the crude phenol acidification tower and the sodium carbonate treatment tower is in countercurrent contact with the tail gas introduced from the bottom in the packing layer, and a small amount of phenol which is brought out when phenolate decomposition is carried out on flue gas in the tail gas is neutralized by using alkali remained in the clean sodium phenolate in the washing procedure, so that the dephenolization and washing effects on the tail gas are achieved;
then the sodium phenolate is automatically fed into the bottom of the middle section of the decomposition tower by utilizing the self gravity, and the sodium phenolate is in parallel-flow contact with carbon dioxide gas entering from the bottom in the tower for bubbling mass transfer to generate a chemical reaction to generate a phenolic substance and sodium carbonate;
the reaction product flows from the upper part of the middle section of the tower to the bottom of the lower section of the decomposition tower in full flow, and continues to carry out decomposition reaction with carbon dioxide blown in from the bottom of the tower;
3) secondary decomposition:
the reaction product which flows out from the upper part of the lower section of the decomposition tower is discharged into a primary decomposition separation tank for oil-water separation, the separated primary decomposed phenol is pumped into the top of the upper section of the crude phenol acidification tower by a primary decomposed phenol pump to be sprayed downwards, the spraying amount is controlled by a liquid level regulating valve, and the separated primary decomposed phenol is in countercurrent contact with tail gas introduced from the bottom of the crude phenol acidification tower in a packing layer to continuously carry out decomposition reaction;
4) the reaction product is automatically fed into the bottom of the lower-section oil-water separator from the bottom of the upper section of the tower by utilizing the self gravity, the secondary decomposition phenol and the sodium carbonate aqueous solution are separated, the secondary decomposition phenol is purified crude phenol, the secondary decomposition phenol is fully fed into a crude phenol tank, and a small amount of liquid sodium carbonate aqueous solution is fed back to a primary decomposition separation tank for oil-water separation again;
5) oil-water separation:
the sodium carbonate aqueous solution separated by the primary decomposition separation tank is sprayed from the top of the upper section of a sodium carbonate treatment tower by a sodium carbonate working pump, the stability of an oil-water interface is controlled by a pressure regulating valve, the sprayed liquid is in countercurrent contact with flue gas introduced from the bottom of the sodium carbonate aqueous solution in a packing layer and is used for decomposing residual sodium phenolate in the sodium carbonate aqueous solution, the reacted reactant is automatically fed into a lower sodium carbonate oil-water separator by utilizing the self gravity to carry out oil-water separation, the crude phenol amount of the top full flow is fed back to the crude phenol side of the primary decomposition separation tank, and the purified sodium carbonate full flow is fed into the sodium carbonate tank.
Compared with the prior art, the invention has the beneficial effects that:
1) three towers are used for replacing six towers in the original process, three delivery pumps and three liquid level recording and adjusting instruments are reduced, so that a large amount of operation cost is saved, occupied area is reduced, and the intrinsic safety of the whole process is improved.
2) The improved crude phenol acidification tower is divided into an upper section and a lower section, the upper section is a crude phenol acidification section, the original bubbling reaction is changed into filler washing, the secondary decomposition rate of primary decomposition phenol can be improved in principle, and the quality of the crude phenol is improved.
Drawings
FIG. 1 is a schematic diagram of the original system structure and a process schematic diagram.
FIG. 2 is a schematic diagram of the structure and process of the present invention.
In the figure: 1-tail gas washing tower 2-1# decomposing tower 3-2# decomposing tower 4-crude phenol acidification tower 5-sodium carbonate treatment tower 6-sodium carbonate oil-water separation tower 7-primary decomposition separation tank 8-secondary decomposition separation tank 9-sodium carbonate working tank 10-flue gas fan 11-sodium phenolate pump 12-primary decomposition phenol pump 13-secondary decomposition phenol pump 14-sodium carbonate working pump 15-sodium carbonate pump 16-liquid level regulating valve one 17-liquid level regulating valve two 18-liquid level regulating valve three 19-liquid level regulating valve four 20-decomposing tower 21-pressure regulating valve 22-liquid level regulating valve LRC-liquid level recording regulating instrument PRC-pressure recording regulating instrument
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in FIG. 2, the carbon dioxide decomposition system for sodium phenolate comprises a decomposition tower 20, a crude phenol acidification tower 4, a sodium carbonate treatment tower 5 and a primary decomposition separation tank 7.
One decomposition tower 20 is adopted to complete the cleaning of tail gas and the primary decomposition of sodium phenolate, the decomposition tower 20 is divided into an upper section, a middle section and a lower section, the top is a tail gas washing section, the middle is a No. 1 decomposition section, and the bottom is a No. 2 decomposition section.
The improved crude phenol acidification tower 4 with the filler is adopted to complete the secondary decomposition of the primary decomposed phenol and the oil-water separation, the improved crude phenol acidification tower 4 is divided into an upper section and a lower section, the upper section is a crude phenol acidification section, the original bubbling reaction is changed into filler washing, and the lower section is an oil-water separation section.
An improved sodium carbonate treatment tower 5 is adopted to treat the purification and oil-water separation of sodium carbonate, the improved sodium carbonate treatment tower 5 is divided into an upper section and a lower section, the upper section is a sodium carbonate treatment section, and the lower section is an oil-water separation section.
The flue gas pipeline is provided with a flue gas fan 10, the flue gas pipeline is respectively connected with the middle section of the decomposition tower 20, the lower section of the decomposition tower 20, the upper section of the crude phenol acidification tower 4 and the upper section of the sodium carbonate treatment tower 5 through branch pipelines thereof,
the upper section of the crude phenol acidification tower 4 is connected with the middle section of the decomposition tower 20 through a pipeline, and the upper section of the sodium carbonate treatment tower 5 is connected with the middle section of the decomposition tower 20 through a pipeline. The middle section of the decomposing tower 20 is connected with the primary decomposing and separating tank 7 through a pipeline, the lower section of the crude phenol acidifying tower 4 is connected with the primary decomposing and separating tank 7 through a pipeline, and the lower section of the sodium carbonate treating tower 5 is connected with the primary decomposing and separating tank 7 through a pipeline. The pipeline connecting the primary decomposition separation tank 7 and the sodium carbonate treatment tower 5 is provided with a sodium carbonate working pump 14 and a pressure regulating valve 21, and the pipeline connecting the primary decomposition separation tank 7 and the crude phenol acidification tower 4 is provided with a primary decomposition phenol pump 12 and a liquid level regulating valve 22.
A carbon dioxide decomposition process of sodium phenolate specifically comprises the following steps:
1) the carbon dioxide-containing flue gas sent from the flue gas pipeline is boosted by the flue gas fan 10 and then sent to the middle section and the lower section of the decomposition tower 20, the upper section of the crude phenol acidification tower 4 and the upper section of the sodium carbonate treatment tower 5 for decomposing sodium phenolate in the liquid phase.
2) The clean sodium phenolate in the clean sodium phenolate tank is pumped into the upper section of the decomposition tower 20, the middle section and the lower section which are introduced from the bottom, the tail gas after phenolate decomposition of the crude phenol acidification tower 4 and the sodium carbonate treatment tower 5 are sprayed from the top and washed, and the tail gas which is introduced from the bottom is in countercurrent contact with the tail gas introduced from the bottom in the packing layer, and a small amount of phenol which is brought out when phenolate decomposition is carried out on the flue gas in the clean sodium phenolate tank is neutralized by using alkali which is remained in the clean sodium phenolate tank in the washing process, so.
Then the sodium phenolate is automatically fed into the bottom of the middle section of the decomposition tower 20 by utilizing the self gravity, and the sodium phenolate is in parallel-flow contact with carbon dioxide gas entering from the bottom in the tower for bubbling mass transfer to generate a chemical reaction to generate a phenolic substance and sodium carbonate; the reaction product flows from the upper part of the middle section of the column to the bottom of the lower section of the decomposition column 20, where it continues the decomposition reaction with carbon dioxide blown in from the bottom of the column, which is called primary decomposition.
3) The reaction product flowing out from the upper part of the lower section of the tower is discharged into a primary decomposition separation tank 7 for oil-water separation, primary decomposed phenol floats on the liquid surface and flows to the other side through an internal partition plate, the separated primary decomposed phenol is sent into the top of the upper section of a crude phenol acidification tower 4 by a primary decomposed phenol pump 12 to be sprayed downwards, the liquid level of LRC-01 is kept constant by a liquid level regulating valve 22 to control the spraying amount, and the separated primary decomposed phenol is in countercurrent contact with tail gas introduced from the bottom of the tower in a packing layer to continuously carry out decomposition reaction, the process is called secondary decomposition and is also a decomposition and purification process of residual sodium phenolate in the crude phenol;
4) the reaction product is automatically fed into the bottom of the lower oil-water separator from the bottom of the upper section of the tower by utilizing the self gravity, the secondary decomposition phenol and the sodium carbonate aqueous solution are separated, the secondary decomposition phenol is purified crude phenol, the crude phenol is fully fed into the crude phenol tank, and a small amount of liquid sodium carbonate aqueous solution is fed back to the primary decomposition separation tank 7 for oil-water separation again.
In order to ensure that the quality of the crude phenol of the oil-water separator at the lower section of the crude phenol acidification tower 4 is absolutely qualified, and the amount of sodium carbonate is small, and the full flow of the sodium carbonate can carry a small amount of crude phenol, the sodium carbonate returns to the primary decomposition separation tank 7 to carry out oil-water separation again.
5) The sodium carbonate aqueous solution separated from the primary decomposition separation tank 7 is sent to the top of the upper section of a sodium carbonate treatment tower 5 by a sodium carbonate working pump 14 to be sprayed, the stability of an oil-water interface is controlled by controlling the pressure PRC-01 of a pipeline in front of the sodium carbonate working pump 14 by a pressure regulating valve 21, a spraying liquid is in countercurrent contact with flue gas introduced from the bottom of the spraying liquid in a packing layer and is used for decomposing residual sodium phenolate in the sodium carbonate aqueous solution, a reactant after reaction is automatically sent to a sodium carbonate oil-water separator at the lower section by utilizing the self gravity to carry out oil-water separation, the crude phenol amount of the top full flow is little and is sent back to the crude phenol side of the primary decomposition separation tank 7, and the purified sodium carbonate.
In order to ensure that the content of the phenol in the sodium carbonate of the oil-water separator at the lower section of the sodium carbonate treatment tower 5 is as small as possible, and the content of the crude phenol is small, and the full flow of the crude phenol possibly contains a small amount of sodium carbonate, the sodium carbonate returns to the crude phenol side of the primary decomposition separation tank 7 and is mixed with the primary decomposition phenol again to be removed to the crude phenol acidification tower for secondary decomposition.
The extraction amount of the sodium carbonate in the primary decomposition separation tank 7 is adjusted by adjusting the pressure of an extraction pipeline, so that the stability of an oil-water separation interface is adjusted, and the extraction quality of the sodium carbonate is further stabilized.
The invention adopts a decomposition tower 20 to complete the cleaning of tail gas and the primary decomposition of sodium phenolate, adopts an improved crude phenol acidification tower 4 with filler to complete the secondary decomposition and oil-water separation of primary decomposed phenol, improves the decomposition rate of phenolate, adopts an improved sodium carbonate treatment tower 5 to treat the purification and oil-water separation of sodium carbonate, and adopts three towers to replace six towers in the original flow, thereby reducing three delivery pumps and three liquid level recording and adjusting instruments, saving a large amount of operation cost, reducing occupied land, and improving the phenolate decomposition rate and the intrinsic safety of the whole process.
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 (7)
1. The carbon dioxide decomposition system of sodium phenolate is characterized by comprising a decomposition tower, a crude phenol acidification tower, a sodium carbonate treatment tower and a primary decomposition separation tank, wherein the decomposition tower is divided into an upper section, a middle section and a lower section;
the flue gas pipeline is respectively connected with the middle section of the decomposition tower, the lower section of the decomposition tower, the upper section of the crude phenol acidification tower and the upper section of the sodium carbonate treatment tower through branch pipelines, the upper section of the crude phenol acidification tower is connected with the middle section of the decomposition tower through a pipeline, and the upper section of the sodium carbonate treatment tower is connected with the middle section of the decomposition tower through a pipeline; the decomposition tower, the crude phenol acidification tower and the sodium carbonate treatment tower are respectively connected with the primary decomposition separation tank through pipelines.
2. The system of claim 1, wherein the flue gas duct is provided with a flue gas blower.
3. The system for decomposing sodium phenolate with carbon dioxide as claimed in claim 1, wherein a sodium carbonate working pump and a pressure regulating valve are provided on a pipeline connecting said primary decomposition separation tank and said sodium carbonate treatment tower, and a primary decomposition phenol pump and a liquid level regulating valve are provided on a pipeline connecting said primary decomposition separation tank and said crude phenol acidification tower.
4. The system for decomposing sodium phenolate with carbon dioxide according to claim 1, wherein said decomposing tower is divided into an upper section, a middle section and a lower section, the top section is a tail gas washing section, the middle section is a # 1 decomposing section, and the bottom section is a # 2 decomposing section.
5. The system for decomposing carbon dioxide into sodium phenolate according to claim 1, wherein said crude phenol acidification tower has an upper section and a lower section, the upper section is a crude phenol acidification section, a filler is provided inside the upper section, and the lower section is an oil-water separation section.
6. The system for decomposing carbon dioxide into sodium phenolate according to claim 1, wherein said sodium carbonate treatment column is divided into an upper section and a lower section, the upper section being a sodium carbonate treatment section, and the lower section being an oil-water separation section.
7. A process based on the system for decomposing carbon dioxide of sodium phenolate according to claim 1, 2, 3, 4, 5 or 6, characterized by comprising the following steps:
1) the flue gas containing carbon dioxide is pressurized by a flue gas fan and then sent into the middle section and the lower section of a decomposing tower, the upper section of a crude phenol acidification tower and the upper section of a sodium carbonate treatment tower,
2) primary decomposition:
the clean sodium phenolate is sent into the decomposing tower from the upper section of the decomposing tower, tail gas after phenolate decomposition of the middle section and the lower section which are introduced from the top and washed from the bottom, the crude phenol acidification tower and the sodium carbonate treatment tower is in countercurrent contact with the tail gas introduced from the bottom in the packing layer, and a small amount of phenol which is brought out when phenolate decomposition is carried out on flue gas in the tail gas is neutralized by using alkali remained in the clean sodium phenolate in the washing procedure, so that the dephenolization and washing effects on the tail gas are achieved;
then the sodium phenolate is automatically fed into the bottom of the middle section of the decomposition tower by utilizing the self gravity, and the sodium phenolate is in parallel-flow contact with carbon dioxide gas entering from the bottom in the tower for bubbling mass transfer to generate phenolic substances and sodium carbonate;
the reaction product flows from the upper part of the middle section of the tower to the bottom of the lower section of the decomposition tower in full flow, and continues to carry out decomposition reaction with carbon dioxide blown in from the bottom of the tower;
3) secondary decomposition:
the reaction product which flows out from the upper part of the lower section of the decomposition tower is discharged into a primary decomposition separation tank for oil-water separation, the separated primary decomposed phenol is pumped into the top of the upper section of the crude phenol acidification tower by a primary decomposed phenol pump to be sprayed downwards, the spraying amount is controlled by a liquid level regulating valve, and the separated primary decomposed phenol is in countercurrent contact with tail gas introduced from the bottom of the crude phenol acidification tower in a packing layer to continuously carry out decomposition reaction;
4) the reaction product is automatically fed into the bottom of the lower-section oil-water separator from the bottom of the upper section of the tower by utilizing the self gravity, the secondary decomposition phenol and the sodium carbonate aqueous solution are separated, the secondary decomposition phenol is purified crude phenol, the secondary decomposition phenol is fully fed into a crude phenol tank, and a small amount of liquid sodium carbonate aqueous solution is fed back to a primary decomposition separation tank for oil-water separation again;
5) oil-water separation:
the sodium carbonate aqueous solution separated by the primary decomposition separation tank is sprayed from the top of the upper section of a sodium carbonate treatment tower by a sodium carbonate working pump, the stability of an oil-water interface is controlled by a pressure regulating valve, the sprayed liquid is in countercurrent contact with flue gas introduced from the bottom of the sodium carbonate aqueous solution in a packing layer and is used for decomposing residual sodium phenolate in the sodium carbonate aqueous solution, the reacted reactant is automatically fed into a lower sodium carbonate oil-water separator by utilizing the self gravity to carry out oil-water separation, the crude phenol amount of the top full flow is fed back to the crude phenol side of the primary decomposition separation tank, and the purified sodium carbonate full flow is fed into the sodium carbonate tank.
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