CN102381943B - System and technology for producing coked crude phenol - Google Patents
System and technology for producing coked crude phenol Download PDFInfo
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- CN102381943B CN102381943B CN201110252781.XA CN201110252781A CN102381943B CN 102381943 B CN102381943 B CN 102381943B CN 201110252781 A CN201110252781 A CN 201110252781A CN 102381943 B CN102381943 B CN 102381943B
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- dehydration
- decomposition
- sodium phenolate
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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000005516 engineering process Methods 0.000 title description 4
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 claims abstract description 99
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 87
- 230000018044 dehydration Effects 0.000 claims abstract description 83
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 83
- 238000005406 washing Methods 0.000 claims abstract description 65
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000003546 flue gas Substances 0.000 claims abstract description 7
- 230000007935 neutral effect Effects 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 33
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 24
- 238000004939 coking Methods 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 12
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 9
- 150000002989 phenols Chemical class 0.000 claims description 9
- 239000011800 void material Substances 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 7
- 239000000945 filler Substances 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 2
- 239000000243 solution Substances 0.000 abstract description 10
- 238000005260 corrosion Methods 0.000 abstract description 8
- 230000007797 corrosion Effects 0.000 abstract description 8
- 229910000831 Steel Inorganic materials 0.000 abstract description 5
- 239000010959 steel Substances 0.000 abstract description 5
- 239000002351 wastewater Substances 0.000 abstract description 4
- 238000001816 cooling Methods 0.000 abstract description 3
- 239000012266 salt solution Substances 0.000 abstract description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 abstract 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- 229910000029 sodium carbonate Inorganic materials 0.000 abstract 1
- 235000017550 sodium carbonate Nutrition 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000011280 coal tar Substances 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a system for producing a coked crude phenol. The system is characterized in that a middle-lower part of a washing tower is communicated with a chimney of a tubular furnace. A phenol sodium salt tank is respectively communicated with middle-upper parts of a washing tower and a dehydration tower through a phenol sodium salt pump. An air inlet is arranged at a middle-lower part of the dehydration tower. An air outlet is arranged at an upper part of the dehydration tower. A dehydration intermediate tank is communicated with a middle-upper part of a decomposition tower through a middle pump. A lower part of the dehydration tower is communicated with the dehydration intermediate tank. An upper part of the washing tower is communicated with a middle-lower part of the decomposition tower through a decomposition tower blower fan. An air outlet is arranged at an upper part of the decomposition tower. The middle-lower part of the decomposition tower is communicated with a crude phenol tank. The bottom of the decomposition tower is communicated with a Na2CO3 solution tank. The system has the advantages that acidic waste water production is reduced, and simultaneously, a SO2 solution is transformed into a neutral salt solution, and thus steel equipment corrosion is avoided; in washing and cooling of flue gas, a phenol sodium salt absorbs CO2 and undergoes a preliminary decomposition simultaneously, and thus a decomposition load of the decomposition tower is reduced; decomposition efficiency is improved; and decomposition is thorough.
Description
Technical field
The invention belongs to coal tar deep processing technical field, especially CO
2method is produced in coking crude phenol Technology and is avoided SO in stack gas
2system and technique that corrosion washing tower and minimizing acid waste water produce.
Background technology
In coal tar, general the employing in the mixed fraction of the relatively concentrated carbolic oil of phenol and naphtalene oil mixed fraction or phenol, naphthalene, washing oil of the extraction of aldehydes matter washed phenol to separate in its cut with the NaOH aqueous solution, first make intermediate product sodium phenolate (this process is also washing process), then pass through CO
2sodium phenolate is decomposed and makes crude phenols (this process is also decomposition course).But CO in using stack gas
2while decomposing clean phenol sodium, wherein contain a small amount of SO
2gas 200mg/Nm
3, in washing process, producing a certain amount of waste water, and steel systeming equipment is caused to corrosion, this is a large drawback of this method.
Above-mentioned washing process and the chemical equation of decomposition course are as follows:
C
6H
5OH?+?NaOH?→?C
6H
5ONa?+?H
2O
2C
6H
5ONa?+?CO
2?+?H
2O?→?2C
6H
5OH?+?NaHCO
3
2C
6H
5ONa?+?SO
2?+?H
2O?→?2C
6H
5OH?+?Na
2SO
3
In the face of SO
2the problem of corrosion washer, current domestic tar source mill all adopts the washer of acid corrosion-resistant, but expensive, has increased production cost.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of CO
2method is produced the novel method of coking crude phenol, to reduce the acid SO of generation and prevention of washes
2gaseous corrosion steel washer.
In order to solve the problems of the technologies described above by the following technical solutions: a kind of production system of coking crude phenol, comprise washing tower, dehydration tower and decomposition tower, the middle and lower part of washing tower and tube furnace chimney are communicated with, and sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively by sodium phenolate pump; Dehydration tower middle and lower part is provided with air intlet, and dehydration tower top is provided with evacuation port, and dehydration medial launder is communicated with by the middle and upper part of line pump and decomposition tower, and dehydration tower bottom and dehydration medial launder are communicated with; Washing tower top is communicated with by decomposition tower blower fan and decomposition tower middle and lower part, and decomposition tower top is provided with evacuation port, and decomposition tower middle and lower part is communicated with crude phenols groove, and decomposition tower bottom is communicated with NaHCO3 solution tank.
Washing tower bottom and sodium phenolate groove are communicated with formation circulation; Dehydration medial launder is also communicated with dehydration tower middle and upper part and is formed circulation by line pump.
Sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively by sodium phenolate pump and interchanger; Dehydration medial launder is communicated with the middle and upper part of dehydration tower and decomposition tower respectively by line pump and interchanger.
Adopt the washing tower that material is 316L, the filler in washing tower is Pall ring, and washing tower specific liquid rate is 20-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Adopt the dehydration tower that material is 316L, the filler in dehydration tower is Pall ring, and dehydration tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Adopt the decomposition tower that material is 316L, the filler in decomposition tower is Pall ring, and decomposition tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1.
Described Pall ring material is 316L.
The production technique of coking crude phenol is as follows: A, flue gas desulfurization (FGD): from the SO that contains of tube furnace chimney
2stack gas enter washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into washing tower middle and upper part from sodium phenolate groove by sodium phenolate pump, the two is counter current contact in washing tower, the SO in stack gas
2by sodium phenolate, absorbed and to be converted into neutral sulfite, and SO in sodium phenolate absorption from flue gas
2rear generation phenol, the simultaneously CO in sodium phenolate and stack gas
2reaction generates phenol; B, sodium phenolate dehydration: another part sodium phenolate in sodium phenolate groove is squeezed into dehydration tower middle and upper part by sodium phenolate pump, dehydration tower middle and lower part enters dry gas by air intlet, the two is counter current contact in tower, after moisture in dry gas absorption portion sodium phenolate, from dehydration tower top, be discharged in atmosphere, sodium phenolate flows into dehydration medial launder by dehydration tower lower part outlet; C, sodium phenolate decompose: in dehydration medial launder, a part of sodium phenolate is squeezed into decomposition tower middle and upper part by line pump, from washing tower top out deviate from SO
2after stack gas under the power of decomposition tower blower fan, enter decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2reaction generates phenol and NaHCO3, and NaHCO3 enters NaHCO3 solution tank from decomposition tower bottom extraction, and phenol enters crude phenols groove from the extraction of decomposition tower middle and lower part, and stack gases is discharged in atmosphere by decomposing tower top.
In steps A, sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in washing tower, and control flow is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control enters washing tower is 60-70 ℃; The effluent gas temperature that goes out washing tower is 50-60 ℃.
In step B, sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in dehydration tower, and controlling sodium phenolate flow is 2-2.5m
3/ h; The flow of controlling dry gas is 5-6m
3/ h.
In step C, between dehydration medial launder and decomposition tower, an interchanger is installed, the temperature that control enters sodium phenolate in decomposition tower is 70-80 ℃; The sodium phenolate concentration that control enters decomposition tower is 30-40%; Decomposition course CO
2pressure-controlling is at 0.03-0.06Mpa, and control decomposition temperature is less than 90 ℃, and sodium phenolate flow is 2-2.5m
3/ h, absorbs with sodium phenolate containing phenol 30-40 wt %.
Decomposition temperature is 80-90 ℃.
Utilization of the present invention is produced the intermediate product sodium phenolate solution producing in crude phenols production process and is replaced water coolant to carry out wash cooling stack gas, has reduced the generation of acid waste water, simultaneously by SO
2be converted into neutral salt solution, avoided steel systeming equipment corrosion.Sodium phenolate, in the process of wash cooling stack gas, absorbs CO simultaneously
2tentatively decompose, reduced the decomposition load of decomposition tower.Improved decomposition efficiency, decomposed more thorough.
Accompanying drawing explanation
Fig. 1 is system flowchart of the present invention.
Reference numeral: 1, tube furnace, 2, washing tower, 3, dehydration tower, 4, decomposition tower, 5, sodium phenolate groove, 6, dehydration medial launder, 7, crude phenols groove, 8, interchanger, 9, interchanger, 10, sodium phenolate pump, 11, line pump, 12, decomposition tower blower fan, 13, air intlet, 14, dehydration tower evacuation port, 15, decomposition tower evacuation port, 16, NaHCO3 solution tank.
Specific embodiments
Below in conjunction with accompanying drawing 1, describe the specific embodiment of the present invention in detail.
As shown in Figure 1, a kind of production system of coking crude phenol, comprise that material is the decomposition tower 4 that the washing tower 2 of 316L, dehydration tower 3 that material is 316L and material are 316L, the middle and lower part of washing tower 2 and tube furnace 1 chimney are communicated with, sodium phenolate groove 5 is communicated with the middle and upper part of washing tower 2 and dehydration tower 3 respectively by sodium phenolate pump 10 and interchanger 8, and washing tower 2 bottoms and sodium phenolate groove 5 are communicated with formation circulation; Dehydration tower 4 middle and lower parts are provided with air intlet 13, dehydration tower 3 tops are provided with dehydration tower evacuation port 14, dehydration medial launder 6 is communicated with the middle and upper part of dehydration tower 3 and decomposition tower 4 respectively by line pump 11 and interchanger 9, and dehydration tower 3 bottoms and dehydration medial launder 6 are communicated with formation circulation; Washing tower 2 tops are communicated with by decomposition tower blower fan 12 and decomposition tower 4 middle and lower parts, and decomposition tower 4 tops are provided with decomposition tower evacuation port 15, and decomposition tower 4 middle and lower parts are communicated with crude phenols groove 7, and decomposition tower 4 bottoms are communicated with NaHCO3 solution tank 16.
It is 316L Pall ring that filler in washing tower, dehydration tower and decomposition tower is material, and washing tower specific liquid rate is 20-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Dehydration tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Decomposition tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1.
The production technique of coking crude phenol is as follows: A, flue gas desulfurization (FGD): from the SO that contains of tube furnace chimney
2(SO
2content 200mg/Nm
3) stack gas enter washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into washing tower middle and upper part from sodium phenolate groove by sodium phenolate pump, the two is counter current contact in washing tower, the SO in stack gas
2by sodium phenolate, absorbed and to be converted into neutral sulfite, thereby avoided the corrosion to steel washing tower, and SO in sodium phenolate absorption from flue gas
2rear generation phenol takes full advantage of again SO when avoiding etching apparatus
2acidity, turn waste into wealth, simultaneously the CO in sodium phenolate and stack gas
2reaction generates phenol, has carried out preliminary decomposition, can alleviate the load that secondary decomposes, and has improved CO
2utilization ratio and decomposition efficiency, strengthened decomposition effect; Sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in washing tower, and control flow is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control enters washing tower is 60-70 ℃; The effluent gas temperature that goes out washing tower is 50-60 ℃.
B, sodium phenolate dehydration: another part sodium phenolate in sodium phenolate groove is squeezed into dehydration tower middle and upper part by sodium phenolate pump, dehydration tower middle and lower part enters dry gas by air intlet, the two is counter current contact in tower, after moisture in dry gas absorption portion sodium phenolate, from dehydration tower top, be discharged in atmosphere, sodium phenolate flows into dehydration medial launder by dehydration tower lower part outlet; Sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in dehydration tower, and controlling sodium phenolate flow is 2-2.5m
3/ h; The flow of controlling dry gas is 5-6m
3/ h.
C, sodium phenolate decompose: in dehydration medial launder, a part of sodium phenolate is squeezed into decomposition tower middle and upper part by line pump, from washing tower top out deviate from SO
2after stack gas under the power of decomposition tower blower fan, enter decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2reaction generates phenol and NaHCO3, and NaHCO3 enters NaHCO3 solution tank from decomposition tower bottom extraction, and phenol enters crude phenols groove from the extraction of decomposition tower middle and lower part, and stack gases is discharged in atmosphere by decomposing tower top; Between dehydration medial launder and decomposition tower, an interchanger is installed, the temperature that control enters sodium phenolate in decomposition tower is 70-80 ℃; The sodium phenolate concentration that control enters decomposition tower is 30-40%; Decomposition course CO
2pressure-controlling is at 0.03-0.06Mpa, and control decomposition temperature is less than 90 ℃, and sodium phenolate flow is 2-2.5m
3/ h, absorbs with sodium phenolate containing phenol 30-40 wt %.
Sodium phenolate produces containing the washing process of phenol cut at NaOH solution washing, and stack gas produces after by tube furnace burning coal gas.In step C, the preferred 80-90 ℃ of decomposition temperature.
Claims (10)
1. a production system for coking crude phenol, is characterized in that: comprise washing tower, dehydration tower and decomposition tower, the middle and lower part of washing tower and tube furnace chimney are communicated with, and sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively by sodium phenolate pump; Dehydration tower middle and lower part is provided with air intlet, and dehydration tower top is provided with evacuation port, and dehydration medial launder is communicated with by the middle and upper part of line pump and decomposition tower, and dehydration tower bottom and dehydration medial launder are communicated with; Washing tower top is communicated with by decomposition tower blower fan and decomposition tower middle and lower part, and decomposition tower top is provided with evacuation port, and decomposition tower middle and lower part is communicated with crude phenols groove, decomposition tower bottom and NaHCO
3solution tank is communicated with.
2. the production system of coking crude phenol according to claim 1, is characterized in that: washing tower bottom and sodium phenolate groove are communicated with formation circulation; Dehydration medial launder is also communicated with dehydration tower middle and upper part and is formed circulation by line pump.
3. the production system of coking crude phenol according to claim 2, is characterized in that: sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively by sodium phenolate pump and interchanger; Dehydration medial launder is communicated with the middle and upper part of dehydration tower and decomposition tower respectively by line pump and interchanger.
4. the production system of coking crude phenol according to claim 1, is characterized in that: adopt the washing tower that material is 316L, the filler in washing tower is Pall ring, and washing tower specific liquid rate is 20-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Adopt the dehydration tower that material is 316L, the filler in dehydration tower is Pall ring, and dehydration tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1; Adopt the decomposition tower that material is 316L, the filler in decomposition tower is Pall ring, and decomposition tower specific liquid rate is 10-50 ton/m
2, void tower air speed is 0.5-1.5ms
-1.
5. the production system of coking crude phenol according to claim 4, is characterized in that: described Pall ring material is 316L.
6. according to the production system of the coking crude phenol described in any one in claim 1,2,3,4,5, it is characterized in that production technique is as follows: A, flue gas desulfurization (FGD): from the SO that contains of tube furnace chimney
2stack gas enter washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into washing tower middle and upper part from sodium phenolate groove by sodium phenolate pump, the two is counter current contact in washing tower, the SO in stack gas
2by sodium phenolate, absorbed and to be converted into neutral sulfite, and SO in sodium phenolate absorption from flue gas
2rear generation phenol, the simultaneously CO in sodium phenolate and stack gas
2reaction generates phenol; B, sodium phenolate dehydration: another part sodium phenolate in sodium phenolate groove is squeezed into dehydration tower middle and upper part by sodium phenolate pump, dehydration tower middle and lower part enters dry gas by air intlet, the two is counter current contact in tower, after moisture in dry gas absorption portion sodium phenolate, from dehydration tower top, be discharged in atmosphere, sodium phenolate flows into dehydration medial launder by dehydration tower lower part outlet; C, sodium phenolate decompose: in dehydration medial launder, a part of sodium phenolate is squeezed into decomposition tower middle and upper part by line pump, from washing tower top out deviate from SO
2after stack gas under the power of decomposition tower blower fan, enter decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2reaction generates phenol and NaHCO3, and NaHCO3 enters NaHCO3 solution tank from decomposition tower bottom extraction, and phenol enters crude phenols groove from the extraction of decomposition tower middle and lower part, and stack gases is discharged in atmosphere by decomposing tower top.
7. the production system of coking crude phenol according to claim 6, is characterized in that: in steps A, sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in washing tower, and control flow is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control enters washing tower is 60-70 ℃; The effluent gas temperature that goes out washing tower is 50-60 ℃.
8. the production system of coking crude phenol according to claim 6, is characterized in that: in step B, sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in dehydration tower, and controlling sodium phenolate flow is 2-2.5m
3/ h; The flow of controlling dry gas is 5-6m
3/ h.
9. the production system of coking crude phenol according to claim 6, is characterized in that: in step C, between dehydration medial launder and decomposition tower, an interchanger is installed, the temperature that control enters sodium phenolate in decomposition tower is 70-80 ℃; The sodium phenolate concentration that control enters decomposition tower is 30-40%; Decomposition course CO
2pressure-controlling is at 0.03-0.06Mpa, and control decomposition temperature is less than 90 ℃, and sodium phenolate flow is 2-2.5m
3/ h, absorbs with sodium phenolate containing phenol 30-40 wt %.
10. the production system of coking crude phenol according to claim 9, is characterized in that: decomposition temperature is 80-90 ℃.
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|---|---|---|---|
| CN201110252781.XA CN102381943B (en) | 2011-08-30 | 2011-08-30 | System and technology for producing coked crude phenol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110252781.XA CN102381943B (en) | 2011-08-30 | 2011-08-30 | System and technology for producing coked crude phenol |
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| CN102381943A CN102381943A (en) | 2012-03-21 |
| CN102381943B true CN102381943B (en) | 2014-01-15 |
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ID=45821840
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109651092B (en) * | 2019-01-24 | 2024-01-05 | 山西永东化工股份有限公司 | Clean production method and device for gas circulation coking crude phenol |
| CN109985507A (en) * | 2019-04-30 | 2019-07-09 | 中冶焦耐(大连)工程技术有限公司 | A kind of method and system for realizing phenol salt de using high-sulfur nitrogen flue gas |
| CN110128245A (en) * | 2019-06-12 | 2019-08-16 | 曹健 | A method of crude phenols are produced using hydrogen chloride gas |
| CN112939746A (en) * | 2021-02-04 | 2021-06-11 | 中冶焦耐(大连)工程技术有限公司 | Pre-pump mixing tower type continuous washing dephenolizing process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1554631A (en) * | 2003-12-22 | 2004-12-15 | 济南钢铁集团总公司 | Process for producing crude carbolic acid by decomposing by-product phenate of coking plant |
| CN101642660A (en) * | 2009-09-02 | 2010-02-10 | 山西宏特煤化工有限公司 | Method for treating exhaust gas in process of producing crude phenol from coal tar |
-
2011
- 2011-08-30 CN CN201110252781.XA patent/CN102381943B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1554631A (en) * | 2003-12-22 | 2004-12-15 | 济南钢铁集团总公司 | Process for producing crude carbolic acid by decomposing by-product phenate of coking plant |
| CN101642660A (en) * | 2009-09-02 | 2010-02-10 | 山西宏特煤化工有限公司 | Method for treating exhaust gas in process of producing crude phenol from coal tar |
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