CN201952379U - Continuous refining and separating device of gasified crude phenol - Google Patents
Continuous refining and separating device of gasified crude phenol Download PDFInfo
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- CN201952379U CN201952379U CN2011200679527U CN201120067952U CN201952379U CN 201952379 U CN201952379 U CN 201952379U CN 2011200679527 U CN2011200679527 U CN 2011200679527U CN 201120067952 U CN201120067952 U CN 201120067952U CN 201952379 U CN201952379 U CN 201952379U
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Abstract
The utility model discloses a continuous refining and separating device of gasified crude phenol, comprising a primary pretreatment acid addition unit, a secondary pretreatment oxidation unit and a refining tower system. The primary pretreatment acid addition unit comprises a scraped film evaporator, a primary acid regulating tank and a buffer tank; the secondary pretreatment oxidation unit comprises a static mixer and a secondary acid regulating tank; and the refining tower system comprises a deslagging tower, a dewatering tower, a phenol refining tower, an o-cresol refining tower and a m-cresol and p-cresol refining tower. The primary pretreatment acid addition unit is connected to a dephenolizing slag tower which is connected to the secondary pretreatment oxidation unit and then sequentially connected to various refining towers. The procedures of bleaching, deodorization, desulfurization and impurity removal are effectively carried out on a gasified crude phenol raw material to obtain the following products: more than 99.5 wt% of high-purity phenol, more than 96.0wt% of high-purity o-cresol, more than 99.0wt% of high-purity m-cresol and p-cresol and mixed xylenol and phenol residue. The utility model has the advantages of reasonable process flow, high degree of automation, low process energy consumption, high product quality, good stability, and the like, and is a high-efficiency practicable continuous refining and separating device of gasified crude phenol.
Description
Technical field
The utility model relates to a kind of refining plant of gasification crude phenols, the isolating device of especially a kind of gasification crude phenols continuous rectification.
Background technology
The gasification phenols is one of main Chemicals of extracting from Coal-gas Washing Water Using and coal tar, and the productive rate of gasification crude phenols is relevant with gasification feed coal character and gasification operation condition thereof with composition.In the Coal Chemical Industry industry, its source of gasification crude phenols comes from the phenolic compound that extracts that produces from coal gasification course on the one hand from phenolic wastewater, come from the carbolic oil cut that coal tar fractional distillation produces on the other hand, the crude phenols component in two sources substantially all contains phenol, ortho-cresol, M-and P-cresols, xylenol, higher phenols and water, neutral wet goods impurity.
Coal Gasification Technology is the important channel and the means of clean utilization coal resources.Pressurizing block Coal Gasification Technology with the Lu Qiwei representative.The lurgi pressure gasification technology in the nineteen thirty exploitation, belongs to first-generation Coal Gasification Technology by Germany LURGI, and technology maturation is reliable, once is maximum Coal Gasification Technology of founding the factory in the world.The strange gasification technology in Shandong is the heart equipment of producing in town gas and the synthetic gas device, characteristics such as the coal that it has adaptation is wide, gasification intensity is big, gasification efficiency height.
From coal gasification course, reclaim the crude phenols history of existing five more than ten years, the equal utility model in various countries multiple recovery and handle the technology of crude phenols.Present fine purification treatment process about phenolic compound, most treating processes that all relate to chemosynthesis phenol, seldom relate to the continuous processing of gasification crude phenols, have only the continuous treating tripping device of Chinese patent coking crude phenols and tripping device and the method that method (CN200910228047.2) discloses the continuous rectification of a kind of coking crude phenols in the domestic document, though also taked a series of pretreatment process at continuous processing, but in whole process since phenol residual oil in a large amount of higher phenolss by sulfate pollution, so can't carry out the subsequent disposal utilization again, cause a large amount of wastings of resources, and in pre-treatment acid adjustment process, because the hysteresis quality of the unstable of crude phenols raw material and detection feedback, cause the fluctuation instability of crude phenols raw material PH after the acid adjustment, can't guarantee that PH is in the best scope all the time, and then influencing the continous-stable that takes off slag effect and a whole set of technology of subsequent technique, obvious this method is not suitable for the continous-stable of the gasification crude phenols that higher phenols can effectively utilize and handles.
Also there is Japanese Patent JP62-12731 to adopt hydrogen peroxide and clay-treated method to come the pre-treatment crude phenols in the document abroad, the compounds such as mercaptan of raw material can be converted into the less disulphide of stink and obtain refining crude phenols by clay-treated method then, experiment shows, this pretreated deodorization and sweetening effectiveness are better, but the poor effect of its decolouring, and the quality product rather unstable behind refining crude phenols is having a strong impact on the refining effect and the recovery value of gasification crude phenols.
Though crude phenols raw material total amount shared ratio in the Coal Chemical Industry product population is less, but modern Coal Chemical Industry industry, especially Zhong Guo Coal Chemical Industry industry size is very huge, the crude phenols raw material total amount of a corresponding Coal Chemical Industry project has also reached more than tens thousand of tonnes, therefore relevant enterprise institute employing equipment is simple both at home and abroad before, invest less intermittent type rectification under vacuum technology, adopt two towers or three tower batch fractionating tower apparatus and technology to finish exactly and take off slag, dehydration, phenol is refining, the technology of plurality of processes such as the refining and xylenol of cresols is refining can't satisfy the needs of huge treatment capacity like this far away.As everyone knows, because the process characteristic of batch fractionating and the thermo-sensitivity characteristic of phenolic compound thereof, make that certainly existing phenolic compound in the batch fractionating separating technology decomposes, polymerization, coking, thereby phenomenons such as carbonization influence the quality and the yield of product, so that the less stable of the quality product of whole technology, simultaneously in the batch fractionating treating processes between its each component interim fraction needs on the high side repeat rectifying and also cause the energy consumption of whole sepn process bigger, obviously from reliability of technology and economy, the technology extensive processing gasification crude phenols preferably that separate crude phenols are made with extra care in continuous rectification.
Summary of the invention
Technical problem to be solved in the utility model is, provides that all phenolic compounds in a kind of crude phenols all can be utilized effectively, good product quality, good stability and the high gasification crude phenols continuous industry of level of automation divide from device; Use this technology that high-purity phenol, ortho-cresol, M-and P-cresols, dimethylphenol can be provided and be not subjected to the products such as phenol residual oil of sulfate pollution.
In order to solve the problems of the technologies described above, the technical solution adopted in the utility model is: a kind of continuous treating tripping device of gasification crude phenols, comprise that the one-level pre-treatment adds sour device, secondary pre-treatment oxidation unit is by taking off the rectifying tower system that slag tower, dehydration tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower constitute; The one-level pre-treatment adds sour device and connects dephenolize slag tower, and dephenolize slag tower connects secondary pre-treatment oxidation unit, connects each rectifying tower system of dehydration tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower then successively; The one-level pre-treatment adds sour device and is made up of the acid adjustment jar group and the surge tank of luwa evaporator, continuously discharging, luwa evaporator top is provided with the crude phenols raw material inlet, the luwa evaporator bottom is provided with slag-drip opening, the luwa evaporator top is provided with the gas phase discharge port, the gas phase discharge port that the luwa evaporator top is provided with connects an acid adjustment jar group, material enters surge tank after acid adjustment jar group and concentrated acid stir, heat, surge tank is communicated with the opening for feed of dephenolize slag tower.
Described secondary pre-treatment oxidation unit is made up of static mixer and secondary acid adjustment jar, dephenolize slag tower bottom is provided with sludge discharge tube, the overhead fraction discharging pipeline of dephenolize slag top of tower and oxygenant pipeline merge after static mixer enters the opening for feed of secondary acid adjustment jar one end, the discharging pipeline that the secondary acid adjustment jar the other end is provided with is connected with the middle part opening for feed of dehydration tower, and the bottom of secondary acid adjustment jar is provided with the acid sludge relief outlet; Dehydration column overhead connects the discharging pipeline of waste water, discharging pipeline at the bottom of the dehydration Tata is connected with the feeding line at phenol treating tower middle part, the discharging pipeline connects the middle part of ortho-cresol treating tower at the bottom of the tower of phenol treating tower, phenol treating tower top connects the discharging pipeline of phenol product, the discharging pipeline is connected with the feeding line at M-and P-cresols treating tower middle part at the bottom of the tower of ortho-cresol treating tower, ortho-cresol treating tower top connects the discharging pipeline of ortho-cresol product, M-and P-cresols treating tower top connects the discharging pipeline of M-and P-cresols product, and M-and P-cresols treating tower bottom connects xylenol crude product discharging pipeline.
A described acid adjustment jar group is made up of the acid adjustment jar of 3 parallel connections at least, has at least one to be in the charging stage in the acid adjustment jar, and one is in agitation phases, and one is in the discharging stage.
A described acid adjustment jar adopts the inner coil pipe heating.
In the described secondary acid adjustment jar over-pass is housed.
Described dephenolize slag tower adopts the forced cyclic type reboiler, takes off waste water tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower and adopts thermosyphon reboiler.
The device of whole separating technology is chosen to be stainless steel, as 304 materials.
The beneficial effects of the utility model are:
1) takes into full account the physicochemical property of gasification crude phenols raw material system, the device of whole separating technology is chosen to be stainless steel, as 304 materials.Thereby the problem of material corrosion resistance nature in the separating technology of having solved has fully guaranteed the quality and the stability of product.
2) the utility model places luwa evaporator before the acid adjustment, and the phenol slag that evaporation is got rid of pollutes without concentrated acid, can reclaim, and as the raw material that the heavy constituent hydrogenation is produced, has saved resource, has reduced pollution.
3) another advantage of the present utility model is exactly to be added sour device and efficiently solved decolouring, desulfurization, the deodorization of crude phenols raw material jointly and taken off problems such as impurity by the secondary pre-treatment oxidation unit that static mixer, secondary acid adjustment jar are formed by the one-level pre-treatment that luwa evaporator, static mixer, acid adjustment jar are formed, and makes that follow-up purified quality product is very high.
4) form of an acid adjustment jar group of employing can guarantee fully carrying out of crude phenols raw material acid adjustment, by time variable control, realizes the continuity operation of technology, has guaranteed the homogeneity that material is formed well, reduces to produce and fluctuates.
5) except that taking off the slag tower, the reboiler of each rectifying tower is all selected thermosyphon reboiler for use, efficiently solve scenes such as phenolic material quick easy decomposition hot in nature, knot carbon, and this rectifying separation automation technolo degree height, process energy consumption are less, for the large-scale continuous production application of gasification crude phenols provides certain advantage, and have favorable economic benefit and social benefit.
The utility model passes through appropriate design, effectively to gasification crude phenols raw material decolour, processes such as deodorization, desulfurization and the removal of impurity, can obtain high purity phenol (＞99.5wt%), high-purity o-phenyl phenol (＞96.0wt%), high-purity Pyrogentisinic Acid (＞99.0wt%) and the xylenol product.Whole process flow is reasonable, level of automation is high and have that the process energy consumption is lower, quality product is high and characteristics such as good stability, is a kind of efficient feasible gasification crude phenols continuous rectification separating technology.
Description of drawings
Fig. 1 is the continuous treating tripping device johning knot composition of gasification crude phenols of the present utility model.
Embodiment
Below in conjunction with the drawings and specific embodiments the utility model is described in further detail:
As shown in Figure 1, the continuous rectification tripping device of gasification crude phenols of the present utility model comprises that the one-level pre-treatment of being made up of luwa evaporator 1, acid adjustment jar group 2 and surge tank 3 adds sour device; Comprise the secondary pre-treatment oxidation unit of forming by static mixer 5 and secondary acid adjustment jar 6; Comprise the rectifying tower system of taking off slag tower 4, dehydration tower 7, phenol treating tower 8, ortho-cresol treating tower 9 and M-and P-cresols treating tower 10.The one-level pre-treatment adds sour device and connects dephenolize slag tower, and dephenolize slag tower connects secondary pre-treatment oxidation unit, connects each rectifying tower system then successively.
An acid adjustment jar group described in the utility model has the function of continuously feeding, acid adjustment, discharge, and concrete structure is as described below: one time acid adjustment jar group is made up of three identical reactors that have stirring and steam tracing, i.e. A/B/C shown in the figure.Adopt mechanical stirring to make material and concentrated acid thorough mixing, adopt steam tracing to make material be warming up to 80 ℃, saved the energy consumption of follow-up flow process.By in the system system, working out corresponding program, the operation of carrying out when realizing charging, stirring, discharging.To be sent to this stage of secondary wiped film vaporization after the acid adjustment and be considered as a complete cycle from once taking off being fed to of crude phenols behind the slag, be 3 hours cycle time.Each complete cycle all is made up of following three minor cycles: the 1) charging stage; 2) agitation phases; 3) the discharging stage.For guaranteeing that three acid adjustment jar flow processs are connected rationally mutually, set each time spent in stage to be 1 hour t.According to according to phase differential principle on the mathematics,, stir and control three acid adjustment jars of A/B/C terminal valve.A jar initial phase is 0h, and then the B jar is 1h, and the C jar is 2h, and the procedure arrangement of each acid adjustment jar and each self-corresponding valve position are referring to table one, table two.
An acid adjustment jar of table one operation is distributed
| Time/sequence number | A | B | C |
| 0-1/3T | Charging | Stir | Discharging |
| 1/3T-2/3T | Stir | Discharging | Charging |
| 2/3T-T | Discharging | Charging | Stir |
An acid adjustment pot valve of table two position distributes
| Valve position/time | 0-1/3T | 1/3T-2/3T | 2/3T-T |
| A jar feed valve | ON | OFF | OFF |
| B jar feed valve | OFF | OFF | ON |
| C jar feed valve | OFF | ON | OFF |
| A jar mechanical stirring | OFF | ON | OFF |
| B jar mechanical stirring | ON | OFF | OFF |
| C jar mechanical stirring | OFF | OFF | ON |
| A jar bleeder valve | OFF | OFF | ON |
| B jar bleeder valve | OFF | ON | OFF |
| C jar bleeder valve | ON | OFF | OFF |
The crude phenols raw material at first enters luwa evaporator 1, and the top of luwa evaporator is provided with liquid phase feeding mouth and gas phase discharge port, and the bottom is provided with phenol slag discharge outlet, and the gas phase discharge port on top is connected to acid adjustment jar group 2 one time, bottom discharge port discharging phenol slag; Concentrated acid enters in acid adjustment jar group and the material of sending here, stirs, steam heating, and fully after the acid adjustment, material enters surge tank 3, and material is delivered to into dephenolize slag tower 4 middle parts by surge tank after the acid adjustment; Dephenolize slag column overhead discharging pipeline and oxidant feed pipeline all are connected to static mixer 5, enter secondary acid adjustment jar from the feeding line on secondary acid adjustment jar 6 tops, secondary acid adjustment jar discharging pipeline is connected to the opening for feed at dehydration tower 7 middle parts, and secondary acid adjustment pot bottom is provided with the acid sludge relief outlet; The dehydration tower top connects the vent line of waste water, and the discharging pipeline of bottom is connected with the feeding line at phenol treating tower 8 middle parts; The phenol tower cat head connects the discharging pipeline of phenol product, and the discharging pipeline of tower bottom is connected to the middle part feeding line of ortho-cresol treating tower 9; The discharging pipeline of the adjoining cresols product of ortho-cresol column overhead, the bottom discharge pipeline is connected with the intermediate feed pipeline of M-and P-cresols treating tower 10; M-and P-cresols treating tower cat head connects the discharging pipeline of M-and P-cresols product, and the bottom connects the discharging pipeline of xylenol crude product.
The separation method of gasification crude phenols of the present utility model continuous rectification, step is as follows:
1) the crude phenols raw material enters luwa evaporator 1, luwa evaporator adopts external jacket formula steam heating, heavy constituent are discharged in the bottom, the gaseous component on top through condensation enter acid adjustment jar group 2 and concentrated acid stir with heat after enter surge tank 3 again, be sent to dephenolize slag tower 4.
2) crude phenols that enter dephenolize slag tower 4 are discharged heavy constituent after treatment at the bottom of the tower, and cat head distilled crude phenols and oxygenant enter static mixer 5, after carrying out the mixed oxidization processing, enter secondary acid adjustment jar 6 then, pot bottom is discharged acid sludge, and the cut that discharge at the top enters dehydration tower 7;
3) dehydration tower 7 tops distillate the waste water that contains a small amount of phenol, and the cut of discharging at the bottom of the tower is to phenol treating tower 8; Phenol product is from the extraction of phenol treating tower, and the cut that discharge phenol treating tower bottom is to ortho-cresol treating tower 9;
4) the ortho-cresol product is from the 9 cat head extraction of ortho-cresol treating tower, and the cut that discharge the bottom is to M-and P-cresols treating tower 10;
5) with extraction, the xylenol cut is discharged in the bottom to the M-and P-cresols product from M-and P-cresols treating tower 10.
Luwa evaporator 1 operational condition of the present utility model is, working pressure is 15Kpa, and chuck adopts the middle pressure steam heating, and the upper gaseous phase temperature out is about 175 ℃.One time acid adjustment jar group 2 is an atmospheric operation, adopts the low-pressure steam heating, and the control of acid adjustment temperature is about 80 ℃, and the mechanical stirring revolution is 60r/min.
Dephenolize slag tower 4 operational conditions of the present utility model are: the cat head working pressure is 10.0～25.0KPa, and reflux ratio is 0.5/1～1/1, and tower top temperature is 110.0～116.0 ℃, and column bottom temperature is 175.0～185.0 ℃; Dehydration slag tower 7 operational conditions are: the cat head working pressure is 10.0～25.0KPa,, reflux ratio is 0.5/1～1/1, and tower top temperature is 58.0～60.0 ℃, and column bottom temperature is 135.0～145.0 ℃; Phenol treating tower 8 operational conditions are: the cat head working pressure is 10.0～25.0KPa, and reflux ratio is 3/1～8/1, and tower top temperature is 120.0～125.0 ℃, and column bottom temperature is 150.0～155.0 ℃; Ortho-cresol treating tower 9 operational conditions are: the cat head working pressure is 10.0～25.0KPa, and reflux ratio is 3/1～6/1, and tower top temperature is 120.0～130.0 ℃, and column bottom temperature is 145.0～160.0 ℃; M-and P-cresols treating tower 10 operational conditions are: the cat head working pressure is 10.0～25.0KPa, and reflux ratio is 4/1～8/1, and tower top temperature is 135.0～140.0 ℃, and column bottom temperature is 155.0～165.0 ℃.
Described concentrated acid is the sulphuric acid soln of 40.0～60.0wt%, and add-on is 3.0～5.0% of a crude phenols material quantity.Described oxygenant is hydrogen peroxide or ozone, and add-on is 1.0～3.0% of a crude phenols amount.
Continuous rectification separating technology of the present utility model adds acid unit, dephenolize slag tower, secondary pre-treatment oxidation unit, dehydration tower, phenol treating tower, ortho-cresol tower and M-and P-cresols tower by the one-level pre-treatment and finishes.
The continuous rectification separating technology of the utility model for forming by five rectifying tower, dephenolize slag Tata internals wherein, rectifying section is efficient structured packing structure, and stripping section is random packing, and all the other four Tata internals are high efficiency structured packing tower.The device of whole separating technology is chosen to be 304 stainless steels, and except that taking off the slag tower, the reboiler of each tower adopts thermosyphon reboiler.
Luwa evaporator 1 operational condition is, working pressure is 15Kpa, and chuck adopts the middle pressure steam heating, and the upper gaseous phase temperature out is about 175 ℃.An acid adjustment jar group (2) is an atmospheric operation, adopts the low-pressure steam heating, and the control of acid adjustment temperature is about 80 ℃, and the mechanical stirring revolution is 60r/min.
Be elaborated below in conjunction with specific embodiment:
Embodiment 1
(flow is 2500.0kg/h to the crude phenols stock liquid that reclaims in the brown coal hydrogasification phenolic wastewater at certain factory of enterprise, component is a phenol 21.7%, ortho-cresol 6.6%, M-and P-cresols 12.1%, water 14.4.0%, xylenol 11.3%, heavy phenol 33.9%), at first the crude phenols stock liquid is entered luwa evaporator, after material enters dephenolize slag tower with gas phase, the bottom is discharged the phenol slag continuously, top distilled crude phenols raw material enters acid adjustment jar group one time with sulphuric acid soln (50.0wt%), add-on is 3.0% of a crude phenols raw material, rotating speed with 60r/min fully stirs an acid adjustment jar group then, be warming up to about 80 ℃, material enters surge tank, after being delivered to dephenolize slag tower, tower bottom is discharged the phenol slag continuously, top distilled crude phenols raw material and hydrogen peroxide solution (30.0wt%) enter static mixer and secondary acid adjustment jar successively, add-on is 1.0% of a crude phenols raw material, secondary acid adjustment jar pot bottom is discharged acid sludge, and crude phenols after treatment enter phenol tower successively, ortho-cresol tower and M-and P-cresols tower.Dephenolize slag tower operational condition is: the cat head working pressure is 10KPa, and reflux ratio is 3/1, and tower top temperature is 108.9 ℃, and column bottom temperature is 177.7 ℃; The dehydration tower operational condition is: the cat head working pressure is 10.0KPa,, reflux ratio is 4/1, and tower top temperature is 45.8 ℃, and column bottom temperature is 120.1 ℃; Phenol treating tower operational condition is: the cat head working pressure is 10.0KPa, and reflux ratio is 10/1, and tower top temperature is 113.6 ℃, and column bottom temperature is 141.3 ℃; Ortho-cresol treating tower operational condition is: the cat head working pressure is 10KPa, and reflux ratio is 9/1, and tower top temperature is 119.5 ℃, and column bottom temperature is 142.8 ℃; M-and P-cresols treating tower operational condition is: the cat head working pressure is 10.0KPa, and reflux ratio is 5/1, and tower top temperature is 131.0 ℃, and column bottom temperature is 148.1 ℃.The technical target of the product that obtains is: phenol (quality product is 99.6wt%, and yield is 98.2%), ortho-cresol (quality product is 98.5wt%, and yield is 99.2%), M-and P-cresols (quality product is 99.1wt%, and yield is 97.5%).
Embodiment 2
(flow is 3750.0kg/h to the crude phenols stock liquid that reclaims in the brown coal pressurized gasification phenolic wastewater at certain factory of enterprise, component is a phenol 27.64%, ortho-cresol 7.92%, M-and P-cresols 23.85%, water 7.63%, xylenol 12.1%, heavy phenol 20.28%), at first the crude phenols stock liquid is entered luwa evaporator, after material enters dephenolize slag tower with gas phase, the bottom is discharged the phenol slag continuously, top distilled crude phenols raw material enters acid adjustment jar group one time with sulphuric acid soln (50.0wt%), add-on is 1.0% of a crude phenols raw material, rotating speed with 60r/min fully stirs an acid adjustment jar group then, be warming up to about 80 ℃, material enters surge tank, be delivered to take off the slag tower after, tower bottom is discharged the phenol slag continuously, top distilled crude phenols raw material and hydrogen peroxide solution (30.0wt%) enter static mixer and secondary acid adjustment jar successively, add-on is 0.5% of a crude phenols raw material, secondary acid adjustment jar pot bottom is discharged acid sludge, and crude phenols after treatment enter successively and take off the xylenol tower, dehydration tower, phenol tower, the cresols knockout tower.Dephenolize slag tower operational condition is: the cat head working pressure is 2.65KPa, and reflux ratio is 2.4/1, and tower top temperature is 67.5 ℃, and column bottom temperature is 127.3 ℃; Taking off xylenol tower operational condition is: the cat head working pressure is 10.0KPa,, reflux ratio is 6/1, and tower top temperature is 113 ℃, and column bottom temperature is 152 ℃; The dehydration tower operational condition is: the cat head working pressure is 18.0KPa,, reflux ratio is 2.5/1, and tower top temperature is 57.7 ℃, and column bottom temperature is 138.1 ℃; Phenol treating tower operational condition is: the cat head working pressure is 10.0KPa, and reflux ratio is 10/1, and tower top temperature is 113.0 ℃, and column bottom temperature is 140.3 ℃; Cresols knockout tower operational condition is: the cat head working pressure is 10.0KPa, and reflux ratio is 8/1, and tower top temperature is 119.4 ℃, and column bottom temperature is 141.7 ℃.The technical target of the product that obtains is: phenol (quality product is 99.6wt%, and yield is 98.2%), ortho-cresol (quality product is 96.5wt%, and yield is 99.2%), M-and P-cresols (quality product is 99.1wt%, and yield is 97.5%).
In sum, content of the present utility model is not limited in the above-described embodiment, knowledgeable people in the same area can propose other embodiment easily within technical director's thought of the present utility model, but this embodiment is included within the scope of the present utility model.
Claims (8)
1. the continuous treating tripping device of gasification crude phenols comprises that the one-level pre-treatment adds sour device, and secondary pre-treatment oxidation unit is by taking off the rectifying tower system that slag tower, dehydration tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower constitute; The one-level pre-treatment adds sour device and connects dephenolize slag tower, and dephenolize slag tower connects secondary pre-treatment oxidation unit, connects each rectifying tower system of dehydration tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower then successively; It is characterized in that: the one-level pre-treatment adds sour device by luwa evaporator (1), an acid adjustment jar group (2) of discharging and surge tank (3) are formed continuously, luwa evaporator (1) top is provided with the crude phenols raw material inlet, luwa evaporator (1) bottom is provided with slag-drip opening, luwa evaporator (1) top is provided with the gas phase discharge port, the gas phase discharge port that luwa evaporator (1) top is provided with connects an acid adjustment jar group (2), material stirs at an acid adjustment jar group (2) and concentrated acid, enter surge tank (3) after the heating, surge tank (3) is communicated with the opening for feed of dephenolize slag tower (4).
2. the continuous treating tripping device of gasification crude phenols according to claim 1, it is characterized in that, described secondary pre-treatment oxidation unit is made up of static mixer (5) and secondary acid adjustment jar (6), dephenolize slag tower (4) bottom is provided with sludge discharge tube, the overhead fraction discharging pipeline at dephenolize slag tower (4) top and oxygenant pipeline merge after static mixer (5) enters the opening for feed of secondary acid adjustment jar (6) one ends, the discharging pipeline that secondary acid adjustment jar (6) the other end is provided with is connected with the middle part opening for feed of dehydration tower (7), and the bottom of secondary acid adjustment jar (6) is provided with the acid sludge relief outlet; Dehydration tower (7) cat head connects the discharging pipeline of waste water, discharging pipeline at the bottom of dehydration tower (7) tower is connected with the feeding line at phenol treating tower (8) middle part, the discharging pipeline connects the middle part of ortho-cresol treating tower (9) at the bottom of the tower of phenol treating tower (8), phenol treating tower (8) top connects the discharging pipeline of phenol product, the discharging pipeline is connected with the feeding line at M-and P-cresols treating tower (10) middle part at the bottom of the tower of ortho-cresol treating tower (9), ortho-cresol treating tower (9) top connects the discharging pipeline of ortho-cresol product, M-and P-cresols treating tower (10) top connects the discharging pipeline of M-and P-cresols product, and M-and P-cresols treating tower (10) bottom connects xylenol crude product discharging pipeline.
3. the continuous treating tripping device of gasification crude phenols according to claim 1 and 2, it is characterized in that a described acid adjustment jar group (2) is made up of the acid adjustment jar of 3 parallel connections at least, have at least one to be in the charging stage in the acid adjustment jar, one is in agitation phases, and one is in the discharging stage.
4. the continuous treating tripping device of gasification crude phenols according to claim 1 is characterized in that, a described acid adjustment jar adopts the heating of steam inner coil pipe.
5. the continuous treating tripping device of gasification crude phenols according to claim 2 is characterized in that, over-pass (11) is housed in the described secondary acid adjustment jar (6).
6. the continuous treating tripping device of gasification crude phenols according to claim 1 and 2, it is characterized in that, described dephenolize slag tower (4) adopts the forced cyclic type reboiler, takes off waste water tower, phenol treating tower, ortho-cresol treating tower and M-and P-cresols treating tower and adopts thermosyphon reboiler.
7. the continuous treating tripping device of gasification crude phenols according to claim 1 and 2 is characterized in that, described continuous treating tripping device is chosen to be stainless steel.
8. the continuous treating tripping device of gasification crude phenols according to claim 7 is characterized in that, described stainless steel is 304 materials.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102584542A (en) * | 2011-12-21 | 2012-07-18 | 江苏泓源化工有限公司 | Method for separating chloro phenol reaction solution |
| CN102731264A (en) * | 2012-07-10 | 2012-10-17 | 陕西省石油化工研究设计院 | Method and device for continuously rectifying and separating medium/low-temperature coal tar crude phenols |
-
2011
- 2011-03-15 CN CN2011200679527U patent/CN201952379U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102584542A (en) * | 2011-12-21 | 2012-07-18 | 江苏泓源化工有限公司 | Method for separating chloro phenol reaction solution |
| CN102584542B (en) * | 2011-12-21 | 2014-04-09 | 江苏泓源化工有限公司 | Method for separating chloro phenol reaction solution |
| CN102731264A (en) * | 2012-07-10 | 2012-10-17 | 陕西省石油化工研究设计院 | Method and device for continuously rectifying and separating medium/low-temperature coal tar crude phenols |
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