CN213537771U - Coking crude phenol production system capable of effectively reducing discharge of three wastes - Google Patents
Coking crude phenol production system capable of effectively reducing discharge of three wastes Download PDFInfo
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- CN213537771U CN213537771U CN202021054377.2U CN202021054377U CN213537771U CN 213537771 U CN213537771 U CN 213537771U CN 202021054377 U CN202021054377 U CN 202021054377U CN 213537771 U CN213537771 U CN 213537771U
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Abstract
The utility model relates to a high temperature coal tar, well low temperature coal tar deep-processing field more specifically, relate to a coking crude phenol production system that can effectively reduce the three wastes and discharge, do not have the three wastes to discharge in the use. Calcium carbonate waste residues are used for producing quicklime in a calcining and causticizing procedure of a calcining kiln, the quicklime is circularly used as a causticizing raw material of sodium carbonate waste liquid, and flue gas of the calcium carbonate calcining kiln is used as a carbon dioxide source for decomposing the sodium phenolate; calcium carbonate waste residues enter a high-temperature flue between a calcium carbonate calcining kiln and a high-temperature ceramic collector, and directly contact with high-temperature flue gas in the high-temperature flue to exchange heat, so that the energy consumption of a system is reduced; treating calcium carbonate waste residues in the causticizing procedure by adopting a high-temperature ceramic collector and a cloth bag collector, and then sending the treated calcium carbonate waste residues into a calcium carbonate calcining kiln; controlling the inlet temperature of the high-temperature ceramic collector and the bag collector by injecting circulating flue gas into inlet pipelines of the high-temperature ceramic collector and the bag collector; the interface height of oil and sodium phenolate in the dephenolizing alkaline washing tower is adjusted by a liquid level regulator.
Description
Technical Field
The utility model relates to a high temperature coal tar, well low temperature coal tar deep-processing field more specifically, relate to a coking crude phenol production system that can effectively reduce the three wastes and discharge.
Background
The production of the coking crude phenol is to distill high-temperature coal tar and medium-low temperature coal tar so as to obtain phenol oil fraction with relatively high phenol content. Then washing the fraction with sodium hydroxide water solution to separate out the phenol substance, the principle is that NaOH reacts with the phenol substance to generate sodium phenolate solution, and the process is also called washing process.
The chemical reaction for washing and dephenolizing is as follows: c6H5OH + NaOH = C6H5ONa + H2O
Crude phenol is then produced by decomposing the sodium salt of phenol with an acidic substance. At present, two methods of carbon dioxide decomposition and sulfuric acid decomposition are mainly adopted in the production of crude phenol by decomposing sodium phenolate in China. The Shandong Dezhou Jinneng Tech Co., Ltd. patent CN102206140A discloses the decomposition with sulfur dioxide gas. When decomposing with sulfur dioxide gas, sulfurous acid is generated due to the presence of water, which severely corrodes equipment, and simultaneously, unreacted sulfur dioxide is discharged into the atmosphere, which has an influence on the environment. When the sodium phenolate is decomposed by the sulfuric acid method, two processes of continuous decomposition and intermittent decomposition are adopted, no matter which process is adopted, sulfuric acid and the sodium phenolate are mixed, the decomposition temperature is controlled to be 80-90 ℃, the phenol content of the sodium phenolate is 20-40%, and when sulfuric acid is added for decomposition, sulfuric acid which does not have a reaction in time exists in the form of dilute sulfuric acid at the local part of equipment, so that the equipment is seriously corroded under the condition. Sodium sulfate waste liquid generated by decomposing sodium phenolate by sulfuric acid method is difficult to treat by the current sewage treatment technology in China, and when sewage is treated by biological method, if the content of sodium sulfate exceeds standard, a large amount of activated sludge can be dead, and the system can be seriously causedAnd the normal operation cannot be performed. When the sodium phenolate is decomposed by the batch process sulfuric acid, because the decomposition process is an exothermic reaction, a large amount of acid mist is generated during the operation of the sulfuric acid decomposition, and the operation environment is seriously influenced. Although there are technical literature disclosing solutions to the above problems associated with persulfuric acid decomposition, such as "acid mist" produced by washing decomposition with sodium phenolate; for Na2SO4Crystallizing the waste liquid, and the like; cannot fundamentally solve the problems of equipment corrosion and environmental pollution caused by 'three wastes'. At present, a carbon dioxide decomposition process is generally adopted, and the requirement of decomposing the sodium phenolate can be met when the concentration of the carbon dioxide reaches 20 percent. Most of the flue gases (active ingredient CO) for industrial use2) Decomposing the sodium salt of phenol. The reaction of carbon dioxide to decompose sodium phenolate is as follows:
C6H5ONa + CO2 + H2O → C6H5OH + NaHCO3
the flue gas is used for decomposing sodium phenolate by utilizing CO in the flue gas2Reacting with sodium phenolate to generate crude phenol and sodium carbonate waste liquor. In order to reduce the environmental pollution caused by the sodium carbonate waste liquid, some factories add Na into quick lime2CO3Waste liquid, CaO and Na2CO3The water in the waste liquid reacts to generate calcium hydroxide, Ca (OH)2Then with Na2CO3Reaction to produce NaOH and Ca2CO3NaOH is circularly used for washing phenol-containing distillate oil to remove phenol, Ca2CO3The precipitate is separated and removed, and the process is called causticization, a chemical reaction formula of causticization.
Na2CO3 + CaO + H2O →CaCO3↓ + 2NaOH
The causticization method is adopted, so that no waste liquid exists in the production process, but Ca exists2CO3Production of waste residues, Ca2CO3The waste residue contains certain harmful substances and still has certain influence on the environment.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the Ca in the prior art2CO3The problem of influence of waste residues on the environment, and provides a method which can realize full cyclic utilization and effectively reduce the discharge of three wastesAnd the production system is used for producing the coking crude phenol by using high-temperature coal tar and medium-low temperature coal tar as raw materials.
In order to solve the technical problem, the utility model discloses the technical scheme who adopts is:
a coking crude phenol production system capable of effectively reducing three-waste discharge is characterized in that: comprises dephenolizing process, decomposing process, causticizing process and calcining process;
the dephenolizing process comprises a dephenolized oil delivery pump and a dephenolizing alkaline washing tower; the dephenolized oil delivery pump is arranged on the ground, an inlet pipeline of the dephenolized oil delivery pump is connected with an external phenol-containing oil pipe and an outlet pipeline of the sodium hydroxide intermediate tank, and an outlet pipeline of the dephenolized oil delivery pump is connected with a material inlet pipeline of the dephenolized alkaline washing tower; the dephenolizing alkaline washing tower is arranged on the ground, a material inlet pipeline at the middle part of the dephenolizing alkaline washing tower is connected with a dephenolizing oil conveying pump outlet pipeline, a dephenolizing oil outlet pipeline at the upper part of the dephenolizing alkaline washing tower is connected with a dephenolizing oil delivery pipeline, and a sodium phenolate outlet pipeline at the bottom of the dephenolizing alkaline washing tower delivers the sodium phenolate to a decomposition process;
the decomposition process comprises a decomposition pump and a decomposition tower; the decomposition pump is arranged on the ground, an inlet pipeline of the decomposition pump is connected with an outlet pipeline of the dephenolizing process, and an outlet of the decomposition pump is connected with an inlet pipeline of the sodium phenolate in the decomposition tower; the decomposing tower is arranged on the ground, a sodium phenolate inlet pipeline of the decomposing tower is connected with a decomposing pump outlet pipeline, two gas inlets of the decomposing tower are connected with a main outlet pipeline of a flue gas induced draft fan, a coking crude phenol outlet pipeline of the decomposing tower is connected with a coking crude phenol outward-sending pipeline, a sodium carbonate waste liquid outlet pipeline of the decomposing tower is connected with a causticizing pump inlet pipeline, and a decomposing tower tail gas connecting pipe is connected with a gas discharge pipeline;
the causticizing procedure comprises a causticizing pump, a causticizer, a filtering dryer, a sodium hydroxide intermediate tank and a calcium carbonate waste residue conveyor; the dephenolizing alkaline washing tower is arranged on the ground, a material inlet pipeline at the middle part of the dephenolizing alkaline washing tower is connected with a dephenolizing oil conveying pump outlet pipeline, a dephenolizing oil outlet pipeline at the upper part of the dephenolizing alkaline washing tower is connected with a dephenolizing oil delivery pipeline, and a sodium phenolate outlet pipeline at the bottom of the dephenolizing alkaline washing tower is connected with a liquid level regulator inlet pipeline; the causticizing pump is arranged on the ground, an inlet pipeline of the causticizing pump is connected with a sodium carbonate waste liquid outlet pipeline of the decomposing tower, and an outlet pipeline of the causticizing pump is connected with a causticizer liquid inlet pipeline; the causticizer is arranged above the filter dryer, a liquid inlet pipeline of the causticizer is connected with a causticizer outlet pipeline, a calcium oxide inlet of the causticizer is connected with a discharge port of a calcium oxide conveyor, and a discharge port at the bottom of the causticizer is connected with a material inlet of the filter dryer; the filtering dryer is arranged above the sodium hydroxide intermediate tank, a material inlet of the filtering dryer is connected with a discharge outlet at the bottom of the causticizer, a liquid material outlet pipeline of the filtering dryer is connected with an inlet pipeline of the sodium hydroxide intermediate tank, and a slag discharge outlet of the filtering dryer is connected with a material inlet at the bottom of the calcium carbonate waste slag conveyor; the sodium hydroxide intermediate tank is arranged on the ground, an inlet pipeline of the sodium hydroxide intermediate tank is connected with a liquid material outlet pipeline of the filtering dryer, a material outlet pipeline of the sodium hydroxide intermediate tank is connected with an inlet pipeline of the dephenolized oil conveying pump, and a supplement material port pipeline of the sodium hydroxide intermediate tank is connected with an external sodium hydroxide pipeline; the bottom material inlet of the calcium carbonate waste residue conveyor is connected with a slag discharge port of the filtering and drying machine, and the top material outlet of the calcium carbonate waste residue conveyor is connected with the material inlet of the raw material bin;
the calcining procedure comprises a calcium carbonate calcining kiln, a raw material bin, a high-temperature ceramic collector, a finished product bin and a calcium oxide conveyor; the calcium carbonate waste residue conveyor conveys calcium carbonate waste residue in a causticization procedure to a raw material bin, a material outlet of the raw material bin conveys the calcium carbonate waste residue to a high-temperature ceramic collector, the calcium carbonate waste residue is conveyed to a calcining section of a calcium carbonate calcining kiln through the high-temperature ceramic collector, raw calcium carbonate is added from the lower part of the calcining section of the calcium carbonate calcining kiln, the raw calcium carbonate is contacted with high-temperature flue gas in the calcining section and is fluidized and calcined, and the calcium carbonate rapidly reacts to generate quicklime and carbon dioxide and enters an expanding section of the calcium carbonate calcining kiln; in the expanding section, due to the reduction of the gas velocity, most of quicklime is precipitated to the deposition area, quicklime powder which is not precipitated enters the collecting section to be further collected and returns to the deposition area, and the generated quicklime enters the deposition area and then enters a finished product bin through a discharging pipe of the deposition area, is stored and cooled in the finished product bin, and is conveyed to a causticizing process by a calcium oxide conveyor to be recycled.
Further, the calcium carbonate calcining kiln adopts a fluidized bed calcining kiln.
Furthermore, a liquid level regulator is also arranged in the dephenolizing process, the upper part of the liquid level regulator is as high as the upper part of the dephenolizing alkaline tower, a material inlet pipeline of the liquid level regulator is connected with a sodium phenolate outlet pipeline of the dephenolizing alkaline tower, and an outlet pipeline of the liquid level regulator is connected with an inlet pipeline of a decomposition pump.
Furthermore, a cloth bag collector, an air/flue gas heat exchanger, a feeder and an air blower are also arranged in the calcining procedure; the bottom of the cloth bag collector is as high as the high-temperature ceramic collector, a flue gas inlet pipeline of the cloth bag collector is connected with a flue gas outlet pipeline of the air/flue gas heat exchanger, a flue gas outlet pipeline of the cloth bag collector is connected with an inlet pipeline of a flue gas induced draft fan, and a discharge port of the cloth bag collector is connected with a material inlet of a feeder; three discharge ports of the cloth bag collector are arranged side by side; the flue gas inlet pipeline of the air/flue gas heat exchanger is connected with the outlet pipeline of the high-temperature ceramic collector, the flue gas outlet pipeline is connected with the inlet pipeline of the cloth bag collector, the air inlet pipeline is connected with the outlet pipeline of the air blower, and the air outlet pipeline is connected with the air pipeline of the calcium carbonate calcining kiln burner; the feeder is arranged below the cloth bag collector and the high-temperature ceramic collector, a material inlet of the feeder is respectively connected with the high-temperature ceramic collector and a material outlet of the cloth bag collector, and a material outlet of the feeder is connected with a raw material inlet of a calcining section of the calcium carbonate calcining kiln; the air blower is installed on the ground, the inlet of the air blower is connected with the atmosphere, and the outlet pipeline is connected with the air inlet pipeline of the air/flue gas heat exchanger.
Furthermore, a flue gas draught fan is further arranged in the calcining procedure, the flue gas draught fan is installed on the ground, an inlet pipeline of the flue gas draught fan is connected with an outlet flue gas pipeline of a calcining procedure collecting mechanism, an outlet main pipeline of the flue gas draught fan is connected with inlets of two gas pipelines of a decomposing tower, and an outlet circulating pipeline of the flue gas draught fan is respectively connected with a lower gas injection port of an expansion section of the calcium carbonate calcining kiln, a lower gas injection port of a collecting section of the calcium carbonate calcining kiln, and a circulating gas injection port of a high-temperature.
Further, the lower gas injection port of the expansion section of the calcium carbonate calcining kiln is set to be 3, and the lower gas injection port of the collection section is set to be 1.
Further, former feed bin includes first former feed bin and the former feed bin of second, calcium carbonate waste residue that comes from the causticization process is received and stored to first former feed bin, the former feed bin of second is connected with the calcium carbonate powder discharge opening for receive and store outsourcing calcium carbonate powder, and calcium carbonate mixes as the calcination raw materials in first former feed bin and the former feed bin of second and sends to the high temperature flue between the high temperature ceramic collector to calcium carbonate calcining kiln.
Further, calcium carbonate in the raw material bin is used as a calcining raw material and is in direct contact with high-temperature flue gas for heat exchange in a high-temperature flue, the high-temperature flue is arranged between the calcium carbonate calcining kiln and the high-temperature ceramic remover, and then the calcium carbonate is conveyed to a calcining section of the calcium carbonate calcining kiln through the high-temperature ceramic collector.
Furthermore, SXF-200 star-shaped feeding valves are respectively arranged at the lower parts of the first raw material bin and the second raw material bin, and the quantity and the proportion of calcium carbonate waste residues in the calcined raw materials and outsourcing calcium carbonate powder are controlled by using speed regulating devices of the feeding valves.
Compared with the prior art, the utility model discloses the beneficial effect who has does:
the utility model provides a coking crude phenol production system capable of effectively reducing the discharge of three wastes, which adopts a fluidized bed calcining kiln to calcine calcium carbonate waste residue in the causticizing procedure to produce quicklime, the quicklime is circularly used as a causticizing raw material of sodium carbonate waste liquid, and the flue gas of the calcium carbonate calcining kiln is used as a carbon dioxide source for decomposing phenol sodium salt; calcium carbonate waste residues enter a high-temperature flue between a calcium carbonate calcining kiln and a high-temperature ceramic collector, and directly contact with high-temperature flue gas in the high-temperature flue to exchange heat, so that the energy consumption of a system is reduced; treating calcium carbonate waste residues in the causticizing procedure by adopting a high-temperature ceramic collector and a cloth bag collector, and then sending the treated calcium carbonate waste residues into a calcium carbonate calcining kiln; controlling the inlet temperature of the high-temperature ceramic collector and the bag collector by injecting circulating flue gas into inlet pipelines of the high-temperature ceramic collector and the bag collector; adjusting the interface height of oil and sodium phenolate in the dephenolizing alkaline washing tower through a liquid level regulator; the utility model discloses the production system who records does not have the three wastes to discharge in the use, has advantages such as automatic level height, convenient operation, energy-concerving and environment-protective, investment province, economic benefits are good, has solved the pollution problem of coking coarse phenol production to the environment and has obvious economic benefits.
Drawings
Figure 1 is the utility model discloses low emission coking crude phenol production system schematic diagram.
In the figure: p101 is a dephenolized oil delivery pump, K101 is a dephenolized alkaline tower, J101 is a liquid level regulator, P201 is a decomposition pump, K201 is a decomposition tower, P301 is a causticizing pump, J301 is a causticizing device, S301 is a filtering dryer, T301 is a sodium hydroxide intermediate tank, S302 is a calcium carbonate waste residue conveyor, Y401 is a calcium carbonate calcining kiln, T401 is a first raw material bin, T402 is a second raw material bin, E401 is an air/flue gas heat exchanger, M401 is a high-temperature ceramic collector, M402 is a cloth bag collector, J401 is a feeder, T403 is a finished product bin, S401 is a calcium oxide conveyor, L401 is a flue gas induced draft fan, L402 is an air blower, 1 is an external phenol-containing oil pipeline, 2 is a dephenolized oil external delivery pipeline, 3 is a coking crude phenol external delivery pipeline, 4 is a gas discharge pipeline, 5 is a calcium carbonate powder discharge port, 6 is an external gas pipeline, 7 is atmospheric air, 8 is an external sodium hydroxide pipeline, A is a calcining section, and B is an expanding section, C is a collecting section and D is a deposition area.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The production method of the coking crude phenol of the utility model is as follows:
(1) washing phenol-containing distillate oil to remove phenol and extract phenol sodium salt:
distilling high-temperature coal tar or medium-low temperature coal tar to obtain phenol oil fraction with 6-20% of phenol content, mixing the phenol oil fraction with NaOH aqueous solution with the mass percentage concentration of 10-15% from a causticization procedure before a dephenolizing oil delivery pump P101, delivering the mixture to the middle part of a dephenolizing alkaline tower K101, reacting the NaOH and phenolic substances to generate a sodium phenolate solution, and separating oil products with phenol removed and sodium phenolate in the dephenolizing alkaline tower K101 by means of specific gravity difference to obtain a sodium phenolate solution with the mass percentage concentration of 20-40% and the temperature of 60-80 ℃;
the chemical reaction for washing and dephenolizing is as follows: c6H5OH + NaOH = C6H5ONa + H2O
Returning the oil product after washing and dephenolizing to a high-temperature coal tar processing device from the upper part of a dephenolizing alkaline tower K101 for further processing;
the interface height of oil and sodium phenolate in the dephenolizing alkaline tower K101 is regulated by a liquid level regulator J101, and crude phenol is extracted from the sodium phenolate through the liquid level regulator J101 to a decomposition process; the liquid level height of oil products and sodium phenolate in the dephenolizing alkaline tower K101 is adjusted by a liquid level adjuster J101; the upper part of the liquid level regulator J101 is as high as the upper part of the dephenolizing alkaline washing tower K101, a material inlet pipeline at the lower part of the liquid level regulator J101 is connected with a sodium phenolate outlet pipeline of the dephenolizing alkaline washing tower K101, and an outlet pipeline at the upper part of the liquid level regulator J101 is connected with an inlet pipeline of a decomposition pump P201; and extracting crude phenol from the sodium phenolate through a liquid level regulator J101 to a decomposition process.
In this embodiment, the high temperature coal tar or the medium and low temperature coal tar must be distilled and cut to obtain phenol-containing fractions, the mass percent of phenol in the fractions obtained by distillation and cut from the high temperature coal tar is 6% -10%, and the mass percent of phenol in the fractions obtained by distillation and cut from the medium and low temperature coal tar is 10% -20%.
(2) Decomposing sodium phenolate to prepare crude phenol:
the upper part of a phenolic sodium salt solution decomposition tower K201 with the temperature of 60-80 ℃ and the mass percent concentration of 20-40 percent is decomposed by a decomposition pump P201, in the embodiment, the phenolic sodium salt solution with the concentration of 25 percent flows from top to bottom and is in reverse contact with flue gas from a flue gas induced draft fan in the calcium carbonate calcination process, in the embodiment, the flue gas is from the flue gas generated in the calcium carbonate waste residue calcination process, the flue gas is formed by a flue of the induced draft fan, and the effective component is CO2CO of flue gas2The concentration is about 20-25%; phenol sodium salt is absorbed by CO in flue gas2Crude phenol and sodium carbonate are generated by decomposition and then flow into the bottom of a decomposition tower K201; the reaction of carbon dioxide to decompose sodium phenolate is as follows:
C6H5ONa + CO2 + H2O → C6H5OH + NaHCO3
the material at the bottom of the decomposing tower K201 is statically separated for about 6 hours at the bottom of the decomposing tower according to the specific gravity difference of the crude phenol and the sodium carbonate at the temperature of 60-80 ℃, and the crude phenol and the Na are completed2CO3Separation of the solution, separated Na2CO3The solution is subjected to a causticization procedure, and crude phenol is taken as a product and is discharged out of the device;
（3）Na2CO3preparing NaOH solution by causticizing the solution:
feeding the sodium carbonate solution generated after the sodium phenolate decomposition into a causticizer J301 by using a causticizing pump P301, adding quicklime from a calcium carbonate calcination process under mechanical stirring, mixing the solid quicklime and the sodium carbonate waste liquid according to the mass ratio of 1:1, reacting the quicklime and the sodium carbonate, finishing causticization when the content of sodium carbonate in the sodium carbonate waste liquid is lower than 1.5 percent to generate a sodium hydroxide solution with the mass percentage concentration of 10-15 percent and calcium carbonate waste residues, filtering and separating the sodium hydroxide solution by using a filtering and drying machine S301, feeding the filtrate sodium hydroxide solution to a washing and dephenolization process for recycling, and feeding the filter residue sodium carbonate waste residues to the next process to serve as a raw material for the calcination process;
Na2CO3 +CaO + H2O →CaCO3↓ + 2NaOH
(4) calcining calcium carbonate waste residues to produce quicklime: na (Na)2CO3Calcium carbonate waste residues generated by causticizing the waste liquid are dried and calcined at the temperature of 900-1200 ℃ to generate quicklime and carbon dioxide flue gas with the volume percentage content of 20-25%; the carbon dioxide flue gas is circularly used for decomposing the sodium phenolate to prepare crude phenol; the quicklime can be recycled for Na2CO3The solution is causticized to prepare NaOH.
The method specifically comprises the following steps: conveying the filtered and dried calcium carbonate waste residue to a first raw material bin T401 by a calcium carbonate waste residue conveyor, and introducing outsourced calcium carbonate powder into a second raw material bin T402; the lower parts of the two raw material bins are respectively provided with an SXF-200 star-shaped feeding valve, and the quantity and the proportion of the two raw materials are controlled by a speed regulating device of the SXF-200 series star-shaped feeding valve; when the adding amount of the raw materials is 6 tons/hour, the proportion of calcium carbonate waste residues in the raw materials is 0-100 percent; the raw materials used by the calcium carbonate calcining kiln are directly preheated by high-temperature flue gas in a high-temperature flue between the calcium carbonate calcining kiln and the high-temperature ceramic collector, the proportioned and metered raw materials enter the high-temperature flue between the calcium carbonate calcining kiln with the effective length being not less than 12 meters and the high-temperature ceramic collector, in the embodiment, the high-temperature flue with the length of 15 meters is adopted, the raw materials directly contact with the high-temperature flue gas in the high-temperature flue for heat exchange, the raw materials are heated to 300-400 ℃, and then the raw materials are collected by two stages of a cyclone and a filter bag and are sent to a calcining section of the calcium carbonate calcining kiln; the effective length of the raw material preheating flue is not less than 12 meters, the surface layer of the flue is a metal shell, and the lining is poured by refractory materials with the refractory temperature of 1300 ℃; the raw material calcium carbonate is added from the lower part of the calcining section, contacts with high-temperature flue gas in the calcining section and is fluidized and calcined, and the calcium carbonate rapidly reacts to generate quicklime and carbon dioxide and enters the expanding section; the temperature of the calcining section is controlled between 900 ℃ and 1200 ℃, and the optimal temperature is controlled between 1000 ℃ and 1150 ℃; calcium carbonate calcination chemical reaction formula:
CaCO3 heating ofCaO+CO2
Calcium carbonate calcining kiln: the device consists of a calcining section A, an expanding section B, a collecting section C and a deposition area D; the surface layer is a metal shell, and the lining is formed by pouring and building refractory materials with the refractory temperature of 1500 ℃; height 16 m. In the expanding section B, due to the reduction of the gas velocity, most of quicklime is precipitated to the deposition area D, quicklime powder which is not precipitated enters the collecting section and is further collected and returns to the deposition area D, and the generated quicklime enters the deposition area D, then enters a finished product bin T403 through a discharging pipe of the deposition area D, is stored in the finished product bin T403, is cooled to 60-80 ℃, and is conveyed to a causticizer by a calcium oxide conveyor for recycling. In order to prevent the quicklime from being accumulated in the deposition area, the lower part of the deposition area D is provided with three circulating flue gas injection ports; in order to prevent the high-temperature ceramic collector and the cloth bag collector from being damaged by overtemperature, a flue gas circulating pipeline is arranged at the outlet of a flue gas draught fan, and gas is injected into the inlet pipelines of the high-temperature ceramic collector and the cloth bag collector, the control method is that regulating valves are respectively arranged on the two flue gas circulating pipelines, the regulating valves and the inlets of the two collectors are interlocked and automatically regulated in temperature, the inlet temperature of the high-temperature ceramic collector is controlled to be not higher than 600 ℃, and the inlet temperature of the cloth bag collector is controlled to.
As shown in fig. 1, a coking crude phenol production system capable of effectively reducing three-waste emission comprises a dephenolized oil delivery pump P101, a dephenolized alkaline washing tower K101, a liquid level regulator J101, a decomposition pump P201, a decomposition tower K201, a causticizing pump P301, a causticizing device J301, a filtering dryer S301, a sodium hydroxide intermediate tank T301, a calcium carbonate waste residue conveyor S302, a calcium carbonate calcining kiln Y401, a first raw material bin T401, a second raw material bin T402, an air/flue gas heat exchanger E401, a high-temperature ceramic collector M401, a cloth bag collector M402, a feeder J401, a finished product bin T403, a calcium oxide conveyor S401, a flue gas induced draft fan L401, and an air blower L402; the dephenolized oil delivery pump P101 is installed on the ground, an inlet pipeline of the dephenolized oil delivery pump P101 is connected with an external phenolic oil-containing pipeline 1 and an outlet pipeline of a sodium hydroxide intermediate tank T301, and an outlet pipeline of the dephenolized oil delivery pump P101 is connected with a material inlet pipeline of a dephenolized alkaline tower K101; the dephenolizing alkaline tower K101 is installed on the ground, a material inlet pipeline in the middle of the dephenolizing alkaline tower K101 is connected with a dephenolizing oil delivery pump P101 outlet pipeline, a dephenolizing oil outlet pipeline on the upper part of the dephenolizing alkaline tower K101 is connected with a dephenolizing oil delivery pipeline 2, and a phenolate salt outlet pipeline at the bottom of the dephenolizing alkaline tower K101 is connected with a liquid level regulator J101 inlet pipeline; the upper part of the liquid level regulator J101 and the upper part of the dephenolizing alkaline washing tower K101 are as high as 12 meters, a material inlet pipeline of the liquid level regulator J101 is connected with a sodium phenolate outlet pipeline of the dephenolizing alkaline washing tower K101, and an outlet pipeline of the liquid level regulator J101 is connected with an inlet pipeline of a decomposition pump P201; the decomposition pump is arranged on the ground, an inlet pipeline of the decomposition pump is connected with an outlet pipeline of the liquid level regulator J101, and an outlet of the decomposition pump is connected with an inlet pipeline of a sodium phenolate salt of the decomposition tower K201; a decomposing tower K201 is arranged on the ground, a sodium phenolate inlet pipeline of the decomposing tower K201 is connected with a decomposing pump P201 outlet pipeline, two gas inlets of the decomposing tower K201 are connected with an outlet main pipeline of a flue gas induced draft fan L401, a coking crude phenol outlet pipeline of the decomposing tower K201 is connected with a coking crude phenol outward-sending pipeline 3, a sodium carbonate waste liquid outlet pipeline of the decomposing tower K201 is connected with a causticizing pump P301 inlet pipeline, and a tail gas connecting pipe of the decomposing tower K201 is connected with a gas discharge pipeline 4; the causticizing pump P301 is arranged on the ground, an inlet pipeline of the causticizing pump P301 is connected with a sodium carbonate waste liquor outlet pipeline of the decomposing tower K201, and an outlet pipeline of the causticizing pump P301 is connected with a liquid inlet pipeline of the causticizer J301; the height of the bottom of the causticizer is 13.6 meters, the causticizer is arranged above the filtering dryer S301, a liquid inlet pipeline of the causticizer is connected with an outlet pipeline of a causticizing pump P301, a calcium oxide inlet of the causticizer J301 is connected with a discharge port of a calcium oxide conveyor S401, and a discharge port at the bottom of the causticizer J301 is connected with a material inlet of the filtering dryer S301; the bottom of the filtering dryer S301 is 7 m high and is arranged above the sodium hydroxide intermediate tank T301, a material inlet of the filtering dryer S301 is connected with a discharge outlet at the bottom of the causticizer J301, a liquid material outlet pipeline of the filtering dryer S301 is connected with a pipeline at the inlet of the sodium hydroxide intermediate tank T301, and a slag discharge outlet of the filtering dryer S301 is connected with a material inlet at the bottom of the calcium carbonate waste slag conveyor S302; the sodium hydroxide intermediate tank is arranged on the ground, an inlet pipeline of the sodium hydroxide intermediate tank is connected with an S301 liquid material outlet pipeline of the filtering dryer, a T301 material outlet pipeline of the sodium hydroxide intermediate tank is connected with an inlet pipeline of a dephenolized oil delivery pump P101, and a T301 supplement material port pipeline of the sodium hydroxide intermediate tank is connected with an external sodium hydroxide pipeline 8; the bottom of the calcium carbonate waste residue conveyor S302 is 6.5 meters in height, a material inlet at the bottom of the calcium carbonate waste residue conveyor S302 is connected with a slag discharge port of the filtering dryer S301, and a material outlet at the top of the calcium carbonate waste residue conveyor S302 is connected with a material inlet of the first raw material bin T401; the calcium carbonate calcining kiln Y401 consists of a calcining section A, an expanding section B, a collecting section C and a deposition area D; the surface layer is a metal shell, the lining is formed by pouring and building refractory materials with the fire resistance temperature of 1500 ℃, the height is 16M, the bottom height is 2M, a material inlet of the lining is connected with an outlet of a feeder J401, a burner interface pipeline at the bottom of a calcium carbonate calcining kiln Y401 is connected with an external gas pipeline 6 and an air outlet pipeline of an air/flue gas heat exchanger E401, an exhaust flue of the calcium carbonate calcining kiln Y401 is connected with a gas inlet pipeline of a high-temperature ceramic collector M401, 3 gas injection ports at the lower part of an expansion section B and 1 gas injection port at the lower part of a collection section C are connected with a circulating gas pipeline at an outlet of a flue gas draught fan L401, and a discharge port of the calcium carbonate calcining kiln Y401; the calcium carbonate calcining kiln Y401 adopts a fluidized bed calcining kiln; the first raw material bin T401 and the second raw material bin T402 are arranged side by side, a material inlet of the first raw material bin T401 is connected with a discharge hole of a calcium carbonate waste residue conveyor S302, a material inlet of the second raw material bin T402 is connected with a calcium carbonate powder discharge hole 5, the calcium carbonate powder discharge hole is purchased calcium carbonate, a material outlet is connected with a flue gas pipeline between a calcium carbonate calcining kiln Y401 and a high-temperature ceramic collector M401 to form the calcium carbonate waste residue discharge hole, the two raw materials are mixed and fed during calcining, and the proportion of calcium carbonate waste residue in the raw materials is 0-100%; the bottom of the air/flue gas heat exchanger E401 is 12 meters high, a flue gas inlet pipeline of the air/flue gas heat exchanger E is connected with an outlet pipeline of a high-temperature ceramic collector M401, a flue gas outlet pipeline of the air/flue gas heat exchanger E is connected with an inlet pipeline of a cloth bag collector M402, an air inlet pipeline of the air/flue gas heat exchanger E is connected with an outlet pipeline of an air blower L402, and an air outlet pipeline of the air/flue gas heat exchanger E is; the height of the bottom of the high-temperature ceramic collector M401 is 4 meters, a flue gas inlet pipeline of the high-temperature ceramic collector M401 is connected with a flue gas outlet pipeline of a calcium carbonate calcining kiln Y401, a flue gas outlet pipeline of the high-temperature ceramic collector M401 is connected with a flue gas inlet pipeline of an air/flue gas heat exchanger, and a discharge outlet is connected with a material inlet of a feeder J401; the height of the bottom of the bag collector M402 is 4 meters, a flue gas inlet pipeline of the bag collector M402 is connected with a flue gas outlet pipeline of an air/flue gas heat exchanger E401, a flue gas outlet pipeline of the bag collector M402 is connected with an inlet pipeline of a flue gas induced draft fan L401, and a discharge outlet of the bag collector M402 is connected with a material inlet of a feeder J401; three discharge ports of the cloth bag collector M402 are arranged side by side; the mounting height of the feeder J401 is 3 meters, the feeder J401 is mounted below the cloth bag collector M402 and the high-temperature ceramic collector M401, the material inlet of the feeder J401 is respectively connected with the discharge outlets of the high-temperature ceramic collector M401 and the cloth bag collector M402, and the material outlet of the feeder J401 is connected with the raw material inlet of the calcium carbonate calcining kiln Y401; the bottom of the finished product bin is 2.5 meters in height, a material inlet is connected with a finished product outlet of a calcium carbonate calcining kiln Y401, a discharge outlet of the finished product bin T403 is connected with a feed inlet of a calcium oxide conveyor S401, and calcium oxide in the finished product bin T403 can be delivered for sale; the bottom of the calcium oxide conveyor is 1.8 meters in height, a feed inlet of the calcium oxide conveyor is connected with a discharge outlet of a finished product bin, and the discharge outlet is connected with a calcium oxide inlet of a causticizer; a flue gas induced draft fan L401 is arranged on the ground, an inlet pipeline of the flue gas induced draft fan L401 is connected with an outlet flue gas pipeline of a cloth bag collector M402, an outlet main pipeline of the flue gas induced draft fan L401 is connected with inlets of two gas pipelines of a decomposing tower K201, and an outlet circulating pipeline of the flue gas induced draft fan L401 is respectively connected with 3 gas injection ports at the lower part of an expanding section B of a calcium carbonate calcining kiln Y401, 1 gas injection port at the lower part of a collecting section C and circulating gas injection ports of a high-temperature ceramic collector M401; an air blower L402 is installed on the floor, with its inlet connected to the atmosphere 7 and its outlet duct connected to the air inlet duct of the air/flue gas heat exchanger E401.
The above description has been made in detail only for the preferred embodiment of the present invention, but the present invention is not limited to the above embodiment, and various changes can be made without departing from the spirit of the present invention within the knowledge scope of those skilled in the art, and all such changes are intended to be encompassed by the present invention.
Claims (9)
1. A coking crude phenol production system capable of effectively reducing three-waste discharge is characterized in that: comprises dephenolizing process, decomposing process, causticizing process and calcining process;
the dephenolizing process comprises a dephenolized oil delivery pump (P101) and a dephenolizing alkaline washing tower (K101); the dephenolized oil delivery pump (P101) is installed on the ground, an inlet pipeline of the dephenolized oil delivery pump is connected with an external phenolic oil-containing pipeline (1) and an outlet pipeline of a sodium hydroxide intermediate tank (T301), and an outlet pipeline of the dephenolized oil delivery pump (P101) is connected with a material inlet pipeline of a dephenolized alkaline washing tower (K101); the dephenolizing alkaline washing tower (K101) is installed on the ground, a material inlet pipeline in the middle of the dephenolizing alkaline washing tower (K101) is connected with a dephenolizing oil delivery pump (P101) outlet pipeline, a dephenolizing oil outlet pipeline in the upper part of the dephenolizing alkaline washing tower (K101) is connected with a dephenolizing oil delivery pipeline (2), and a sodium phenolate outlet pipeline at the bottom of the dephenolizing alkaline washing tower (K101) delivers sodium phenolate to a decomposition process;
the decomposition process comprises a decomposition pump (P201) and a decomposition tower (K201); the decomposition pump (P201) is arranged on the ground, an inlet pipeline of the decomposition pump is connected with an outlet pipeline of a dephenolizing process, and an outlet of the decomposition pump is connected with an inlet pipeline of a sodium phenolate salt in the decomposition tower (K201); the decomposition tower (K201) is arranged on the ground, a sodium phenolate inlet pipeline of the decomposition tower (K201) is connected with an outlet pipeline of a decomposition pump (P201), two gas inlets of the decomposition tower (K201) are connected with an outlet main pipeline of a flue gas induced draft fan (L401), a coking crude phenol outlet pipeline of the decomposition tower (K201) is connected with a coking crude phenol outward delivery pipeline (3), a sodium carbonate waste liquid outlet pipeline of the decomposition tower (K201) is connected with an inlet pipeline of a causticizing pump (P301), and a tail gas connecting pipe of the decomposition tower (K201) is connected with a gas discharge pipeline (4);
the causticizing process comprises a causticizing pump (P301), a causticizer (J301), a filter dryer (S301), a sodium hydroxide intermediate tank (T301) and a calcium carbonate waste residue conveyor (S302); a phenol sodium salt outlet pipeline at the bottom of the dephenolizing alkaline tower (K101) is connected with an inlet pipeline of the liquid level regulator (J101); the causticizing pump (P301) is installed on the ground, an inlet pipeline of the causticizing pump is connected with a sodium carbonate waste liquid outlet pipeline of the decomposing tower (K201), and an outlet pipeline of the causticizing pump is connected with a liquid inlet pipeline of the causticizer (J301); the causticizer (J301) is arranged above the filtering dryer (S301), a liquid inlet pipeline of the causticizer (J301) is connected with an outlet pipeline of the causticizing pump (P301), a calcium oxide inlet of the causticizer (J301) is connected with a discharge port of a calcium oxide conveyor (S401), and a discharge port at the bottom of the causticizer (J301) is connected with a material inlet of the filtering dryer (S301); the filtering dryer (S301) is arranged above the sodium hydroxide intermediate tank (T301), a material inlet of the filtering dryer (S301) is connected with a discharge outlet at the bottom of the causticizer (J301), a liquid material outlet pipeline of the filtering dryer (S301) is connected with an inlet pipeline of the sodium hydroxide intermediate tank (T301), and a slag discharge outlet of the filtering dryer (S301) is connected with a material inlet at the bottom of the calcium carbonate waste slag conveyor (S302); the sodium hydroxide intermediate tank (T301) is arranged on the ground, an inlet pipeline of the sodium hydroxide intermediate tank is connected with a liquid material outlet pipeline of the filtering dryer (S301), a material outlet pipeline of the sodium hydroxide intermediate tank (T301) is connected with an inlet pipeline of the dephenolized oil conveying pump (P101), and a supplement material port pipeline of the sodium hydroxide intermediate tank (T301) is connected with an external sodium hydroxide pipeline (8); the material inlet at the bottom of the calcium carbonate waste residue conveyor (S302) is connected with the residue discharge port of the filtering dryer (S301), and the material outlet at the top of the calcium carbonate waste residue conveyor (S302) is connected with the material inlet of the raw material bin;
the calcining process comprises a calcium carbonate calcining kiln (Y401), a raw material bin, a high-temperature ceramic collector (M401), a finished product bin (T403) and a calcium oxide conveyor (S401); the calcium carbonate waste residue conveyor (S302) is used for conveying the calcium carbonate waste residue in the causticizing procedure into a raw material bin; the outlet of the raw material bin is used for conveying calcium carbonate waste residues to a high-temperature ceramic collector (M401); the high-temperature ceramic collector (M401) is used for conveying calcium carbonate waste residues to the lower part of a calcining section (A) of a calcium carbonate calcining kiln (Y401); the calcium carbonate calcining kiln (Y401) consists of a calcining section (A), an expanding section (B), a collecting section (C) and a deposition area (D); the calcining section (A) is used for contacting calcium carbonate with high-temperature flue gas, fluidizing and calcining to generate quicklime and carbon dioxide; the expanding section (B) sinks the quicklime to a deposition area (D) through gas velocity reduction; the collecting section (C) is used for further collecting the quicklime powder which does not settle down and returning the quicklime powder to the sedimentation area (D); the deposition area (D) is used for collecting quicklime; the finished product bin (T403) is used for storing and cooling quicklime powder discharged from a discharging pipe of the deposition area (D); the finished product bin (T403) discharge opening is connected with the feed inlet of the calcium oxide conveyor (S401), and the calcium oxide conveyor (S401) is used for conveying quicklime powder to the causticization process for recycling.
2. The system for producing coked crude phenol with effectively reduced three-waste emission according to claim 1, wherein the calcium carbonate calcining kiln (Y401) is a fluidized bed calcining kiln.
3. The system for producing the coked crude phenol capable of effectively reducing the emission of three wastes according to claim 1, which is characterized in that a liquid level regulator (J101) is further arranged in the dephenolizing process, the upper part of the liquid level regulator (J101) is as high as the upper part of a dephenolizing alkaline washing tower (K101), a material inlet pipeline of the liquid level regulator (J101) is connected with a sodium phenolate outlet pipeline of the dephenolizing alkaline washing tower (K101), and an outlet pipeline of the liquid level regulator (J101) is connected with an inlet pipeline of a decomposition pump (P201).
4. The system for producing the coked crude phenol capable of effectively reducing the emission of three wastes according to claim 1, which is characterized in that a cloth bag collector (M402), an air/flue gas heat exchanger (E401), a feeding machine (J401) and an air blower (L402) are further arranged in the calcining procedure; the bottom of the cloth bag collector (M402) is as high as the high-temperature ceramic collector (M401), a flue gas inlet pipeline of the cloth bag collector (M402) is connected with a flue gas outlet pipeline of an air/flue gas heat exchanger (E401), a flue gas outlet pipeline of the cloth bag collector (M402) is connected with an inlet pipeline of a flue gas induced draft fan (L401), and a discharge port of the cloth bag collector (M402) is connected with a material inlet of a feeder (J401); the discharge openings of the bag collector (M402) are arranged in three in parallel; the flue gas inlet pipeline of the air/flue gas heat exchanger (E401) is connected with the outlet pipeline of the high-temperature ceramic collector (M401), the flue gas outlet pipeline is connected with the inlet pipeline of the cloth bag collector (M402), the air inlet pipeline is connected with the outlet pipeline of the air blower (L402), and the air outlet pipeline is connected with the air pipeline of the calcium carbonate calcining kiln (Y401) burner; the feeding machine (J401) is arranged below the cloth bag collector (M402) and the high-temperature ceramic collector (M401), a material inlet of the feeding machine (J401) is respectively connected with a discharge outlet of the high-temperature ceramic collector (M401) and a discharge outlet of the cloth bag collector (M402), and a material outlet of the feeding machine (J401) is connected with a raw material inlet of a calcining section (A) of the calcium carbonate calcining kiln (Y401); the air blower (L402) is installed on the ground, the inlet of the air blower is connected with the atmosphere (7), and the outlet pipeline is connected with the air inlet pipeline of the air/flue gas heat exchanger (E401).
5. The system for producing coked crude phenol capable of effectively reducing the emission of three wastes according to claim 1, which is characterized in that the flue gas induced draft fan (L401) is installed on the ground, an inlet pipeline of the flue gas induced draft fan is connected with an outlet flue gas pipeline of a calcining process collecting mechanism, an outlet main pipeline of the flue gas induced draft fan (L401) is connected with inlets of two gas pipelines of a decomposing tower (K201), and an outlet circulating pipeline of the flue gas induced draft fan (L401) is respectively connected with a gas injection port at the lower part of an expanding section (B) and a gas injection port at the lower part of a collecting section (C) of a calcium carbonate calcining kiln (Y401) and a circulating gas injection port of a high-temperature.
6. The system for producing coked crude phenol with the effect of reducing the emission of three wastes according to claim 1, wherein the number of gas injection ports at the lower part of the expansion section (B) of the calcium carbonate calcining kiln (Y401) is 3, and the number of gas injection ports at the lower part of the collection section (C) is 1.
7. The system for producing coked crude phenol with the effect of reducing the emission of three wastes according to claim 1, wherein the raw material bin comprises a first raw material bin (T401) and a second raw material bin (T402), the first raw material bin (T401) receives and stores calcium carbonate waste residues from a causticizing process, the second raw material bin (T402) is connected with a calcium carbonate powder discharge opening (5) and is used for receiving and storing purchased calcium carbonate powder, and calcium carbonate in the first raw material bin (T401) and the second raw material bin (T402) is mixed to be used as a calcination raw material and is sent to a high-temperature flue between a calcium carbonate calcination kiln (Y401) and a high-temperature ceramic collector (M401).
8. The system for producing coked crude phenol capable of effectively reducing the emission of three wastes according to claim 1 or 7, characterized in that calcium carbonate in the raw material bin is used as a calcination raw material to directly contact with high-temperature flue gas for heat exchange in a high-temperature flue, the high-temperature flue is arranged between a calcium carbonate calcination kiln (Y401) and a high-temperature ceramic collector (M401), and then the calcium carbonate is conveyed to the calcination section (A) of the calcium carbonate calcination kiln (Y401) through the high-temperature ceramic collector (M401).
9. The system for producing coked crude phenol capable of effectively reducing the emission of three wastes according to claim 7, wherein SXF-200 star-shaped feed valves are respectively installed at the lower parts of the first raw material bin (T401) and the second raw material bin (T402), and the quantity and the proportion of calcium carbonate waste residues in the calcined raw materials and the purchased calcium carbonate powder are controlled by using speed regulating devices of the feed valves.
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