CN102381943A - System and technology for producing coked crude phenol - Google Patents
System and technology for producing coked crude phenol Download PDFInfo
- Publication number
- CN102381943A CN102381943A CN201110252781XA CN201110252781A CN102381943A CN 102381943 A CN102381943 A CN 102381943A CN 201110252781X A CN201110252781X A CN 201110252781XA CN 201110252781 A CN201110252781 A CN 201110252781A CN 102381943 A CN102381943 A CN 102381943A
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- CN
- China
- Prior art keywords
- tower
- dehydration
- decomposition
- sodium phenolate
- communicated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000005516 engineering process Methods 0.000 title description 6
- 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 88
- 230000018044 dehydration Effects 0.000 claims abstract description 81
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 81
- 238000005406 washing Methods 0.000 claims abstract description 64
- 238000004519 manufacturing process Methods 0.000 claims abstract description 21
- 230000007935 neutral effect Effects 0.000 claims abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000003546 flue gas Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 33
- 150000002989 phenols Chemical class 0.000 claims description 26
- 238000004939 coking Methods 0.000 claims description 17
- 239000011734 sodium Substances 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 10
- 239000007788 liquid Substances 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
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 241000282326 Felis catus Species 0.000 claims description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims description 2
- 239000000243 solution Substances 0.000 abstract description 9
- 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
- 239000012141 concentrate 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
- 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 the coal tar deep processing technical field, especially CO
2Avoid SO in the stack gas in the method production coking crude phenols Technology
2System and technology that corrosion washing tower and minimizing acid waste water produce.
Background technology
The extraction of aldehydes matter generally is employed in the mixed fraction of carbolic oil that phenol concentrates relatively and naphtalene oil mixed fraction or phenol, naphthalene, washing oil phenol to be washed in its cut with the NaOH aqueous solution and separates in the coal tar; Make the clean sodium phenolate of intermediate product (this process also is washing process) earlier, pass through CO then
2Clean sodium phenolate decomposition is made crude phenols (this process also is decomposition course).But CO in stack gas
2When 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 corrosion, this is a big drawback of this method.
The above-mentioned washing process and the chemical equation of decomposition course are following:
C
6H
5OH?+?NaOH?→?C
6H
5ONa?+?H
2O
2C
6H
5ONa?+?CO
2?+?H
2O?→?2C
6H
5OH?+?Na
2CO
3
2C
6H
5ONa?+?SO
2?+?H
2O?→?2C
6H
5OH?+?Na
2SO
3
In the face of SO
2The problem of corrosion washer, present domestic tar source mill all adopts the washer of acid corrosion-resistant, but costs an arm and a leg, and has increased production cost.
Summary of the invention
Technical problem to be solved by this invention provides a kind of CO
2The novel method of method production coking crude phenols is with the generation that reduces washes and prevent acid SO
2Gaseous corrosion steel washer.
Adopt following technical scheme in order to solve the problems of the technologies described above: a kind of production system of coking crude phenols; Comprise washing tower, dehydration tower and decomposition tower; The middle and lower part of washing tower and tube furnace chimney are communicated with, and the sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively through the sodium phenolate pump; The dehydration tower middle and lower part is provided with air, and dehydration tower top is provided with evacuation port, and the dehydration medial launder is communicated with through the middle and upper part of line pump and decomposition tower, and the dehydration tower bottom is communicated with the dehydration medial launder; Washing tower top is communicated with through decomposition tower blower fan and decomposition tower middle and lower part, and decomposition tower top is provided with evacuation port, and the decomposition tower middle and lower part is communicated with the crude phenols groove, decomposition tower bottom and Na
2CO
3Solution tank is communicated with.
Scrubbing tower bottom and sodium phenolate groove are communicated with the formation circulation; The dehydration medial launder also is communicated with the formation circulation by line pump with the dehydrating tower middle and upper part.
The sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively through sodium phenolate pump and interchanger; The dehydration medial launder is communicated with the middle and upper part of dehydration tower and decomposition tower respectively through line pump and interchanger.
Adopting material is the washing tower of 316L, and the filler in the washing tower is a Pall ring, and the washing tower specific liquid rate is 20-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; Adopting material is the dehydration tower of 316L, and the filler in the dehydration tower is a Pall ring, and the dehydration tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; Adopting material is the decomposition tower of 316L, and the filler in the decomposition tower is a Pall ring, and the decomposition tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s.
Described Pall ring material is 316L.
The production technique of coking crude phenols is following: A, FGD: from the SO that contains of tube furnace chimney
2Stack gas get into the washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into the washing tower middle and upper part by the sodium phenolate pump from the sodium phenolate groove, the two is counter current contact in washing tower, the SO in the stack gas
2Be converted into neutral sulfite by the sodium phenolate absorption, and the SO in the sodium phenolate absorption from flue gas
2The back generates phenol, simultaneously the CO in sodium phenolate and the stack gas
2Reaction generates phenol; B, sodium phenolate dehydration: another part sodium phenolate in the sodium phenolate groove is squeezed into the dehydration tower middle and upper part by the sodium phenolate pump; The dehydration tower middle and lower part gets into dry gas through air; The two is counter current contact in tower; Be discharged in the atmosphere from dehydration tower top behind the moisture in the dry gas absorption portion sodium phenolate, sodium phenolate then flows into the dehydration medial launder by the dehydration tower lower part outlet; C, sodium phenolate decompose: a part of sodium phenolate is squeezed into the decomposition tower middle and upper part by line pump in the dehydration medial launder, and that comes out from washing tower top deviates from SO
2After stack gas under the power of decomposition tower blower fan, get into the decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2Reaction generates phenol and Na
2CO
3, Na
2CO
3Get into Na from decomposition tower bottom extraction
2CO
3Extraction gets into the crude phenols groove from the decomposition tower middle and lower part for solution tank, phenol, and stack gases is discharged in the atmosphere by decomposing cat head.
In the steps A, clean sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in the washing tower, and dominant discharge is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control gets into washing tower is 60-70 ℃; The effluent gas temperature that goes out washing tower is 50-60 ℃.
Among the step B, sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in the dehydration tower, and control sodium phenolate flow is 2-2.5m
3/ h; The flow of control dry gas is 5-6m
3/ h.
Among the step C, an interchanger is installed between dehydration medial launder and decomposition tower, the temperature that control gets into sodium phenolate in the decomposition tower is 70-80 ℃; The sodium phenolate concentration that control gets into decomposition tower is 30-40%; Decomposition course CO
2Pressure-controlling is at 0.03-0.06Mpa, and the control decomposition temperature is less than 90 ℃, and the sodium phenolate flow is 2-2.5m
3/ h, absorption contains phenol 30-40wt% with sodium phenolate.
Decomposition temperature is 80-90 ℃.
Utilization of the present invention is produced the intermediate product sodium phenolate solution that produces in the crude phenols production process and is replaced water coolant to wash cooling stack gas, has reduced the generation of acid waste water, simultaneously with SO
2Be converted into neutral salt solution, avoided the steel systeming equipment corrosion.Sodium phenolate absorbs CO simultaneously in the process of washing cooling stack gas
2Tentatively decompose, reduced the decomposition load of decomposition tower.Improved decomposition efficiency, decomposed more thorough.
Description of drawings
Fig. 1 is a 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, the dehydration medial launder, 7, the crude phenols groove, 8, interchanger; 9, interchanger, 10, the sodium phenolate pump, 11, line pump, 12, the decomposition tower blower fan; 13, air, 14, the dehydration tower evacuation port, 15, the decomposition tower evacuation port, 16, Na
2CO
3Solution tank.
Specific embodiments
Specify embodiment of the present invention below in conjunction with accompanying drawing 1.
As shown in Figure 1; A kind of production system of coking crude phenols; 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, and sodium phenolate groove 5 is communicated with the middle and upper part of washing tower 2 and dehydration tower 3 respectively through sodium phenolate pump 10 and interchanger 8, and washing tower 2 bottoms and 5 connections of sodium phenolate groove form circulation; Dehydration tower 4 middle and lower parts are provided with air 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 through line pump 11 and interchanger 9, and dehydration tower 3 bottoms are communicated with to form with dehydration medial launder 6 circulates; Washing tower 2 tops are communicated with through 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, decomposition tower 4 bottoms and Na
2CO
3 Solution tank 16 is communicated with.
It is the 316L Pall ring that filler in washing tower, dehydration tower and the decomposition tower is material, and the washing tower specific liquid rate is 20-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; The dehydration tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; The decomposition tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s.
The production technique of coking crude phenols is following: A, FGD: from the SO that contains of tube furnace chimney
2(SO
2Content 200mg/Nm
3) stack gas get into the washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into the washing tower middle and upper part by the sodium phenolate pump from the sodium phenolate groove, the two is counter current contact in washing tower, the SO in the stack gas
2Be converted into neutral sulfite by the sodium phenolate absorption, thereby avoided corrosion the steel washing tower, and the SO in the sodium phenolate absorption from flue gas
2The back generates phenol, when avoiding etching apparatus, has made full use of SO again
2Acidity, turn waste into wealth, simultaneously the CO in sodium phenolate and the 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 the decomposition effect; Clean sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in the washing tower, and dominant discharge is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control gets into 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 the sodium phenolate groove is squeezed into the dehydration tower middle and upper part by the sodium phenolate pump; The dehydration tower middle and lower part gets into dry gas through air; The two is counter current contact in tower; Be discharged in the atmosphere from dehydration tower top behind the moisture in the dry gas absorption portion sodium phenolate, sodium phenolate then flows into the dehydration medial launder by the dehydration tower lower part outlet; Sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in the dehydration tower, and control sodium phenolate flow is 2-2.5m
3/ h; The flow of control dry gas is 5-6m
3/ h.
C, sodium phenolate decompose: a part of sodium phenolate is squeezed into the decomposition tower middle and upper part by line pump in the dehydration medial launder, and that comes out from washing tower top deviates from SO
2After stack gas under the power of decomposition tower blower fan, get into the decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2Reaction generates phenol and Na
2CO
3, Na
2CO
3Get into Na from decomposition tower bottom extraction
2CO
3Extraction gets into the crude phenols groove from the decomposition tower middle and lower part for solution tank, phenol, and stack gases is discharged in the atmosphere by decomposing cat head; An interchanger is installed between dehydration medial launder and decomposition tower, and the temperature that control gets into sodium phenolate in the decomposition tower is 70-80 ℃; The sodium phenolate concentration that control gets into decomposition tower is 30-40%; Decomposition course CO
2Pressure-controlling is at 0.03-0.06Mpa, and the control decomposition temperature is less than 90 ℃, and the sodium phenolate flow is 2-2.5m
3/ h, absorption contains phenol 30-40wt% with sodium phenolate.
Sodium phenolate produces at the washing process that the NaOH solution washing contains the phenol cut, and stack gas produces after by tube furnace burning coal gas.Among the step C, the preferred 80-90 of decomposition temperature ℃.
Claims (10)
1. the production system of coking crude phenols 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 the sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively through the sodium phenolate pump; The dehydration tower middle and lower part is provided with air, and dehydration tower top is provided with evacuation port, and the dehydration medial launder is communicated with through the middle and upper part of line pump and decomposition tower, and the dehydration tower bottom is communicated with the dehydration medial launder; Washing tower top is communicated with through decomposition tower blower fan and decomposition tower middle and lower part, and decomposition tower top is provided with evacuation port, and the decomposition tower middle and lower part is communicated with the crude phenols groove, decomposition tower bottom and Na
2CO
3Solution tank is communicated with.
2. the production system of coking crude phenols according to claim 1 is characterized in that: scrubbing tower bottom and sodium phenolate groove are communicated with the formation circulation; The dehydration medial launder also is communicated with the formation circulation by line pump with the dehydrating tower middle and upper part.
3. the production system of coking crude phenols according to claim 2 is characterized in that: the sodium phenolate groove is communicated with the middle and upper part of washing tower and dehydration tower respectively through sodium phenolate pump and interchanger; The dehydration medial launder is communicated with the middle and upper part of dehydration tower and decomposition tower respectively through line pump and interchanger.
4. the production system of coking crude phenols according to claim 1 is characterized in that: adopting material is the washing tower of 316L, and the filler in the washing tower is a Pall ring, and the washing tower specific liquid rate is 20-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; Adopting material is the dehydration tower of 316L, and the filler in the dehydration tower is a Pall ring, and the dehydration tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s; Adopting material is the decomposition tower of 316L, and the filler in the decomposition tower is a Pall ring, and the decomposition tower specific liquid rate is 10-50 ton/m
2, the void tower air speed is 0.5-1.5m/s.
5. the production system of coking crude phenols according to claim 4 is characterized in that: described Pall ring material is 316L.
6. according to the production system of any described coking crude phenols in the claim 1,2,3,4,5, it is characterized in that production technique is following: A, FGD: from the SO that contains of tube furnace chimney
2Stack gas get into the washing tower middle and lower part, wherein a part of sodium phenolate is squeezed into the washing tower middle and upper part by the sodium phenolate pump from the sodium phenolate groove, the two is counter current contact in washing tower, the SO in the stack gas
2Be converted into neutral sulfite by the sodium phenolate absorption, and the SO in the sodium phenolate absorption from flue gas
2The back generates phenol, simultaneously the CO in sodium phenolate and the stack gas
2Reaction generates phenol; B, sodium phenolate dehydration: another part sodium phenolate in the sodium phenolate groove is squeezed into the dehydration tower middle and upper part by the sodium phenolate pump; The dehydration tower middle and lower part gets into dry gas through air; The two is counter current contact in tower; Be discharged in the atmosphere from dehydration tower top behind the moisture in the dry gas absorption portion sodium phenolate, sodium phenolate then flows into the dehydration medial launder by the dehydration tower lower part outlet; C, sodium phenolate decompose: a part of sodium phenolate is squeezed into the decomposition tower middle and upper part by line pump in the dehydration medial launder, and that comes out from washing tower top deviates from SO
2After stack gas under the power of decomposition tower blower fan, get into the decomposition tower middle and lower part, the two is counter current contact in tower, sodium phenolate and CO
2Reaction generates phenol and Na
2CO
3, Na
2CO
3Get into Na from decomposition tower bottom extraction
2CO
3Extraction gets into the crude phenols groove from the decomposition tower middle and lower part for solution tank, phenol, and stack gases is discharged in the atmosphere by decomposing cat head.
7. the production system of coking crude phenols according to claim 6 is characterized in that: in the steps A, clean sodium phenolate circulates between sodium phenolate groove and washing tower, keeps level stability in the washing tower, and dominant discharge is 2-2.5m
3/ h; An interchanger is installed between sodium phenolate groove and washing tower, and the sodium phenolate temperature that control gets into washing tower is 60-70 ℃; The effluent gas temperature that goes out washing tower is 50-60 ℃.
8. the production system of coking crude phenols according to claim 6 is characterized in that: among the step B, sodium phenolate circulates between dehydration medial launder and dehydration tower, keeps level stability in the dehydration tower, and control sodium phenolate flow is 2-2.5m
3/ h; The flow of control dry gas is 5-6m
3/ h.
9. the production system of coking crude phenols according to claim 6 is characterized in that: among the step C, an interchanger is installed between dehydration medial launder and decomposition tower, the temperature that control gets into sodium phenolate in the decomposition tower is 70-80 ℃; The sodium phenolate concentration that control gets into decomposition tower is 30-40%; Decomposition course CO
2Pressure-controlling is at 0.03-0.06Mpa, and the control decomposition temperature is less than 90 ℃, and the sodium phenolate flow is 2-2.5m
3/ h, absorption contains phenol 30-40wt% with sodium phenolate.
10. the production system of coking crude phenols according to claim 9 is characterized in that: decomposition temperature is 80-90 ℃.
Priority Applications (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 |
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 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102381943A true CN102381943A (en) | 2012-03-21 |
| CN102381943B CN102381943B (en) | 2014-01-15 |
Family
ID=45821840
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110252781.XA Active CN102381943B (en) | 2011-08-30 | 2011-08-30 | System and technology for producing coked crude phenol |
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|---|---|
| CN (1) | CN102381943B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
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| Publication number | Publication date |
|---|---|
| CN102381943B (en) | 2014-01-15 |
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