CN108870413B - Method for incinerating petrochemical waste liquid based on gas and oily liquid mixed fuel - Google Patents
Method for incinerating petrochemical waste liquid based on gas and oily liquid mixed fuel Download PDFInfo
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- CN108870413B CN108870413B CN201710338308.0A CN201710338308A CN108870413B CN 108870413 B CN108870413 B CN 108870413B CN 201710338308 A CN201710338308 A CN 201710338308A CN 108870413 B CN108870413 B CN 108870413B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2204/00—Supplementary heating arrangements
- F23G2204/10—Supplementary heating arrangements using auxiliary fuel
- F23G2204/103—Supplementary heating arrangements using auxiliary fuel gaseous or liquid fuel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/10—Liquid waste
- F23G2209/101—Waste liquor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
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Abstract
The invention discloses a method for incinerating petrochemical waste liquid based on mixed fuel of gas and oily liquid, which comprises the steps of spraying the petrochemical waste liquid into a combustion area of a waste alkali incinerator in an atomization mode, taking fuel gas and oily liquid as combustion-supporting fuel, combusting under the condition of blowing oxygen-containing gas, and controlling the temperature of the combustion area to be 800-1200 ℃; the batch volumes of the petrochemical waste liquid, the fuel gas and the oily liquid meet the following requirements simultaneously: the volume of the petrochemical waste liquid per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.7-1.0 t/h.m2The fuel gas amount per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.05-0.09 t/h.m2(ii) a The amount of the oily liquid per hour/the cross-sectional area of a hearth of a combustion zone of the waste alkali incinerator is 0.03-0.08 t/h.m2. The method can realize reasonable combustion load, reduce treatment cost, reduce the damage of overhigh combustion load to the device and is beneficial to the popularization and application of the waste liquid incineration technology in the industry.
Description
Technical Field
The invention relates to a method for treating petrochemical waste liquid, in particular to a method for incinerating petrochemical waste liquid by using combustible gas and oily fuel at the same time, and belongs to the technical field of petrochemical industry.
Background
The petrochemical industry such as the industrial process for preparing cyclohexanone by oxidizing cyclohexane generates a large amount of high-concentration organic waste alkali liquor, so that the standard treatment of the waste alkali liquor is the bottleneck of energy expansion of the industry. At the end of the last ninety years, the medium petrochemical holy company successfully developed the waste alkali incineration technology based on the alkali recovery furnace method, has the advantages of high COD removal rate, conformity with the national environmental emission standard after treatment and the like, gradually becomes the mainstream technology of cyclohexanone saponification waste alkali treatment, and has been put into application in most of the newly built or expanded cyclohexanone projects in China in recent years.
The cyclohexanone waste lye incineration device has complex sources and various types of auxiliary fuels due to cost consideration and fuel supply limitation, generally adopts industrial byproducts or deep-processed products thereof, and the components and the low calorific value of the industrial byproducts or the deep-processed products thereof are frequently changed, so that the stable combustion and the operation cost of a boiler are influenced; the adjustment of the byproduct steam price also affects the operating economy. Further, the type of fuel used is limited by the supply, and it is sometimes necessary to use all of the oil fuel, and sometimes it is possible to use both the oil fuel and the gas fuel, but sometimes it is only possible to use all of the gas fuel, and the variation in fuel supply causes fluctuation in waste liquid incineration cost, which brings a problem in the control of the facility cost. Therefore, the change of fuel supply is responded by process innovation, and the reduction of the treatment cost is an urgent need of a chemical waste liquid incineration device.
The method comprises spraying and atomizing saponified waste alkali liquor into a high-temperature furnace chamber, drying and decomposing in the furnace chamber, wherein 60-80% of the saponified waste alkali liquor reacts in the furnace chamber to generate sodium carbonate, the sodium carbonate is collected along with flue gas in an electrostatic dust collector, 20-40% of the sodium carbonate falls to the furnace bottom and is combusted at the furnace bottom to generate molten sodium carbonate, and the molten sodium carbonate flows into a dissolving tank through a chute to form liquid alkali. The prior art has the problems that when the fuel source is limited and only gas fuel and oily liquid can be used for waste alkali incineration treatment at the same time: when the mixed fuel is used as the boiler fuel, the fuel proportioning is unreasonably controlled, the process requirement of ultrahigh temperature of a combustion area is caused under the condition of large fuel consumption and incomplete combustion, and the problems of damage of a water wall tube, hardening of a melt on a water screen, blockage of a flue gas channel and the like are easy to occur; when the fuel consumption is insufficient, the incineration conversion rate of the waste liquid is insufficient, the boiler efficiency is reduced, and the waste liquid treatment cannot meet the environmental protection requirement. The unreasonable process proportion causes the fluctuation of the working condition of the device, the driving period is shortened, the waste alkali treatment cost is high, the enthusiasm of enterprises for putting the environment-friendly device is seriously influenced, and the environment protection and emission reduction of the chemical industry are not facilitated.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a method for incinerating petrochemical waste liquid, which realizes reasonable combustion load, reduces treatment cost and reduces the damage of overhigh combustion load to a device by adjusting the gas fuel, the liquid fuel and the petrochemical waste liquid to be in reasonable proportion.
In order to achieve the technical purpose, the invention discloses a method for incinerating petrochemical waste liquid based on mixed fuel of gas and oily liquid, which comprises the steps of incinerating the petrochemical waste liquid by using a waste alkali incinerator, wherein the waste alkali incinerator is an alkali recovery furnace and comprises a water-cooled wall, a water-cooled screen, an evaporation tube screen, a steam pocket, an economizer and an air preheater; the heat generated by the combustion of the petrochemical waste liquid, the gas and the oily liquid mixed fuel heats the furnace water of the waste alkali incinerator to generate byproduct steam; spraying the petrochemical waste liquid into a combustion area of a waste alkali incinerator in an atomization mode, taking fuel gas and oily liquid as combustion-supporting fuel, combusting under the condition of blowing oxygen-containing gas, and controlling the temperature of the combustion area to be 800-1200 ℃; the feeding amount of the petrochemical waste liquid, the fuel gas and the oily liquid meets the following requirements: the volume of the petrochemical waste liquid per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.7-1.0 t/h.m2The fuel gas amount per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.05-0.09 t/h.m2(ii) a The amount of the oily liquid per hour/the cross-sectional area of a hearth of a combustion zone of the waste alkali incinerator is 0.03-0.08 t/h.m2。
Preferably, the pressure of the fuel gas entering the waste alkali incinerator is 50-200 kPa. The fuel gas enters the boiler through the contraction nozzle for combustion, and under the condition of optimal pressure, the gas fuel can be fully mixed with petrochemical waste liquid and oxygen for combustion, so that a good combustion effect is achieved.
In a more preferable scheme, the low-level combustion heat value of the fuel gas is 31260-37840 kj/kg.
In a further preferred scheme, the fuel gas is at least one of refinery dry gas, natural gas and coal bed gas.
Preferably, the pressure of the oily liquid entering the waste alkali incinerator is 0.3-0.7 MPa. Under the action of the pressure, the oily liquid can obtain a good atomization effect, so that the oily liquid has high dispersity, and is fully mixed and combusted with auxiliary gas fuel, oxygen and petrochemical industry waste materials to achieve a good combustion effect.
In a more preferable scheme, the low-level combustion heat value of the oily liquid is 34000-42000 kj/kg.
In a further preferred scheme, the oily liquid is at least one of coal tar, oil refining atmospheric residue and oil refining catalytic cracking slurry oil.
Preferably, the fuel gun for injecting the combustible gas is installed at a height higher than that of the spray gun for injecting the oily liquid. The combustion area can be optimized, the combustion completeness of the waste liquid and the fuel oil is improved, and the combustion of dry solids at the bottom of the combustion furnace is enhanced.
In the preferable scheme, the pressure of the petrochemical waste liquid entering the waste alkali incinerator is 1.4-2.8 MPa. Under the action of the pressure, the petrochemical waste liquid can obtain a good atomization effect, so that the petrochemical waste alkali liquid has high dispersity, and is fully mixed and combusted with auxiliary fuel and oxygen to achieve a good combustion effect.
In a preferable scheme, the petrochemical waste liquid is cyclohexanone waste alkali liquid, the low calorific value of solid matters is 10000-14000 kJ/kg, and the mass percentage content of the solid matters is 30-60%.
In a preferable scheme, heat generated after the petrochemical waste liquid, the fuel gas and the oily liquid are combusted is used for heating furnace water of the waste alkali incinerator, and steam is a byproduct.
In the preferable scheme, the temperature of the combustion zone is 900-1100 ℃.
In a preferable scheme, the flue gas outlet of the waste alkali incinerator is connected with an electric dust remover, and combustion ash from the waste alkali incinerator is deposited and recovered from the tail of the waste alkali incinerator along with flue gas or is captured and recovered by the electric dust remover.
The waste alkali incinerator comprises a water-cooled wall, a water-cooled screen, an evaporation tube screen, a steam drum, an economizer and an air preheater. The combustion area hearth of the waste alkali incinerator is square or approximately square. Two groups of burners are arranged at the lower part in the furnace body of the waste alkali incinerator, and a petrochemical waste liquid ejector is arranged between the two groups of burners. And a chute is arranged at the bottom of the waste alkali incinerator. The fuel gas spray gun is arranged at a position close to the bottom of the hearth, and the installation height of the fuel gas spray gun is higher than that of the oily liquid spray gun.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects:
1) according to the technical scheme, when gas fuel or oily fuel cannot be sufficiently supplied, by simultaneously using the gas fuel and the liquid fuel and strictly controlling the feeding amount ratio of the petrochemical waste liquid to the fuel, the combustion intensity of the cyclohexanone waste alkali and other petrochemical waste liquids can be reasonable when the petrochemical waste liquids are incinerated, the problems of tail gas pollution and even flameout and shutdown caused by low combustion load are avoided, the problems of energy waste and equipment service life reduction caused by overhigh combustion load are solved, the incineration treatment cost of the petrochemical waste liquids can be obviously reduced, the waste liquid incineration environment-friendly device can reliably exert the environment-friendly function, and simultaneously can operate at low cost and even side cost, and the large-scale popularization and application in the whole industry are facilitated.
2) By applying production tests, it follows: the method for treating the cyclohexanone waste alkali liquor by adopting the technology of the invention is about 9.5 ten thousand tons/year on the scale of 10 ten thousand tons/year of cyclohexanone, and compared with the technology of the invention, the method can reduce the treatment cost by 20-78 yuan/ton, the annual reduction cost can reach 190-740 ten thousand yuan, and the cost reduction effect on an environment-friendly device is very outstanding.
Detailed Description
The embodiments of the present invention will be described in detail with reference to examples, which do not indicate specific conditions, and which are performed under conventional conditions or conditions common in the industry.
A10 ten thousand ton grade cyclohexanone waste alkali incineration device comprises a water wall, a water screen, an evaporation tube screen, a steam pocket, an economizer, an air preheater and the like, wherein the size of a square combustion chamber formed by the water wall is 3.85 m multiplied by 3.85 m, and the waste liquid incineration treatment process method comprises the following steps:
pressurizing the waste saponified alkali liquor to 1.8-2.5 MPa, feeding the waste saponified alkali liquor into a saponified liquid spray gun, atomizing the waste saponified alkali liquor, feeding the waste saponified alkali liquor into an alkali recovery boiler, and suspending and drying the waste saponified alkali liquor in the boilerSpace combustion (suspension combustion). Conversion of organic acid sodium salt in saponification liquor to Na2CO3The reaction gives off a large amount of heat.
The auxiliary fuel oil is regulated and stabilized to 0.3-0.7 MPa through a fuel oil pipeline loop, and then enters a furnace through a vapor atomized oil gun for combustion.
And the auxiliary fuel gas is regulated to 50-200 kpa through a fuel gas pipeline loop after being regulated by a gas buffer tank, and is sprayed into the furnace through a fuel gas gun for combustion.
The fuel gas rifle is installed and is being close to boiler furnace bottom position, and the mounting height is higher than supplementary fuel oil spray gun more than 100mm, is favorable to strengthening the bed course degree of combustion to combustible substance burning is in order to improve combustion efficiency in the help flue gas.
The combustion ash is deposited at the tail part of the boiler along with the flue gas or collected and recovered by electric dust removal, and is conveyed to an ash bucket by a scraper conveyor to be packaged and sold, wherein the main component of the recovered ash is sodium carbonate. Larger particles are not ready to burn in the hearth space and fall onto the hearth cushion layer to be burnt out (cushion layer burning). And the generated sodium carbonate melt flows out from a chute opening at the bottom of the waste alkali incineration boiler and enters a solid alkali recovery unit through a chute groove to obtain a crude sodium carbonate byproduct. The flue gas is introduced into a chimney with the height of 80m for evacuation.
The heat released by the combustion reaction in the furnace heats soft water on the heating surfaces of a lower economizer, an upper drum, a boiling tube panel, a lower drum and the like to generate 1.27MPa steam, and the rest of the soft water is merged into a low-pressure steam pipe network outside a boundary area except a small amount of soft water for the device.
The used oily auxiliary fuel is one or more of catalytic slurry oil, residual oil and coal tar, and the fuels have the following properties:
catalytic slurry properties:
| component name | Maximum value | Minimum value | Mean value of |
| Ash content m% | 0.798 | 0.412 | 0.599 |
| Kinematic viscosity (100 ℃ C.), mm2/s | 29.1 | 19.82 | 25.694 |
| Density, kg/m3 | 1190.5 | 1096.9 | 1141.02 |
| Solids content% | 3.3 | 2 | 2.016 |
| Low combustion heat value, kj/kg | 42000 | 36000 | 40000 |
The properties of the residual oil are as follows:
| component name | Maximum value | Minimum value | Mean value of |
| Ash content m% | 0.39 | 0.21 | 0.3 |
| Density, kg/m3 | 1030.4 | 1099.6 | 1065 |
| Low combustion heat value, kj/kg | 42000 | 36000 | 41000 |
The properties of coal tar:
| component name | Maximum value | Minimum value | Mean value of |
| Ash content m% | 4.94 | 2.96 | 3.95 |
| Low combustion heat value, kj/kg | 42560 | 37000 | 39780 |
The fuel gas fuel used is one or more of refinery dry gas, natural gas and coal bed gas, taking the refinery dry gas as an example, the fuel gas fuel has the following properties:
dry gas properties:
the waste liquid after incineration treatment is cyclohexanone saponification waste alkali, and has the following properties:
property of cyclohexanone waste alkali:
| component name | Maximum value | Minimum value | Mean value of |
| Density, kg/m3 | 1310 | 1180 | 1240 |
| Solids content% | 65％ | 35％ | 43％ |
| Low combustion heat value, kj/kg | 11520 | 13260 | 12110 |
The effects of the present invention can be better illustrated by comparing example 1, example 2, example 3 with comparative example 1 in terms of process proportioning conditions and corresponding variable costs, and the relevant data are shown in table 1.
TABLE 1 Process proportioning conditions and corresponding variable costs
In the table, the cost per ton of spent caustic treatment was variable, namely consumption value (clean water + electricity + soft water + residual oil) -by-product value (low pressure steam).
Compared with the comparative example 1, the waste alkali incineration treatment cost of the examples 1, 2 and 3 can be reduced by 20-78 yuan/ton.
The above embodiments are only exemplary embodiments of the present invention, and are not intended to limit the present invention, and the scope of the present invention is defined by the claims. Various modifications and equivalents may be made by those skilled in the art within the spirit and scope of the present invention, and such modifications and equivalents should also be considered as falling within the scope of the present invention.
Claims (13)
1. A method for burning petrochemical waste liquid based on gas and oily liquid mixed fuel adopts a waste alkali incinerator to burn the petrochemical waste liquid, wherein the waste alkali incinerator is an alkali recovery furnace and comprises a water-cooled wall, a water-cooled screen, an evaporation tube screen, a steam drum, an economizer and an air preheater; the heat generated by the combustion of the petrochemical waste liquid, the gas and the oily liquid mixed fuel heats the furnace water of the waste alkali incinerator to generate byproduct steam; the method is characterized in that: spraying the petrochemical waste liquid into a combustion area of a waste alkali incinerator in an atomization mode, taking fuel gas and oily liquid as combustion-supporting fuel, combusting under the condition of blowing oxygen-containing gas, and controlling the temperature of the combustion area to be 800-1200 ℃; the batch volumes of the petrochemical waste liquid, the fuel gas and the oily liquid meet the following requirements simultaneously: the volume of the petrochemical waste liquid per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.7-1.0 t/h.m2The fuel gas amount per hour/the cross-sectional area of the combustion zone hearth of the waste alkali incinerator is 0.05-0.09 t/h.m2The amount of the oily liquid per hour/the cross-sectional area of a hearth of a combustion zone of the waste alkali incinerator is 0.03-0.08 t/h.m2。
2. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 1, wherein: the pressure of the fuel gas entering the waste alkali incinerator is 50-200 kPa.
3. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 2, wherein: the low-level combustion heat value of the fuel gas is 31260-37840 kj/kg.
4. A method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 3, wherein: the fuel gas is at least one of refinery dry gas, natural gas and coal bed gas.
5. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 1, wherein: the pressure of the oily liquid entering the waste alkali incinerator is 0.3-0.7 MPa.
6. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 5, wherein: the low-level combustion heat value of the oily liquid is 34000-42000 kj/kg.
7. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 6, wherein: the oily liquid is at least one of coal tar, oil refining atmospheric residue and oil refining catalytic cracking slurry oil.
8. The method for incinerating a petrochemical waste liquid based on a gas and oily liquid mixed fuel according to any one of claims 1 to 7, characterized in that: the fuel spray gun for spraying combustible gas is higher than the spray gun for spraying oily liquid.
9. The method for incinerating a petrochemical waste liquid based on a gas and oily liquid mixed fuel according to any one of claims 1 to 7, characterized in that: the pressure of the petrochemical waste liquid entering the waste alkali incinerator is 1.4-2.8 MPa.
10. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 9, wherein: the petrochemical waste liquid is cyclohexanone saponification waste lye.
11. The method for incinerating a petrochemical effluent based on a gas and oily liquid mixed fuel according to claim 10, wherein: the solid low-heat value of the cyclohexanone saponification waste alkali liquor is 10000-14000 kJ/kg, and the mass percentage content of the solid is 30-60%.
12. The method for incinerating a petrochemical waste liquid based on a gas and oily liquid mixed fuel according to any one of claims 1 to 7, characterized in that: the temperature of the combustion zone is 900-1100 ℃.
13. The method for incinerating petrochemical waste liquid based on gas and oily liquid mixed fuel according to any one of claims 1 to 7 and 10, characterized in that: the flue gas outlet of the waste alkali incinerator is connected with an electric dust remover, and combustion ash from the waste alkali incinerator is deposited and recovered from the tail of the waste alkali incinerator along with flue gas or is collected and recovered by the electric dust remover.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3946077A (en) * | 1973-03-28 | 1976-03-23 | Bayer Aktiengesellschaft | Process for oxidating hydrocarbons |
| CN1424535A (en) * | 2002-12-20 | 2003-06-18 | 巨化集团公司 | Combustion nozzle for cyelohexanone saponified waste water |
| CN101734824A (en) * | 2008-11-04 | 2010-06-16 | 王富绩 | Process for treating saponifiable waste alkali liquor by chemical method |
| CN102192513A (en) * | 2011-05-25 | 2011-09-21 | 大连科林能源工程技术开发有限公司 | Incinerator of multi-element multi-dimension chemical hazardous waste |
| CN102877351A (en) * | 2011-07-15 | 2013-01-16 | 中国石油化工集团公司 | Treatment method of high concentration waste alkali solution |
| CN103591591A (en) * | 2013-11-06 | 2014-02-19 | 武汉锅炉集团工程技术有限公司 | Saponification waste liquid combustion and alkali recovery boiler |
| CN103822216A (en) * | 2014-03-18 | 2014-05-28 | 江苏星瑞化工工程科技有限公司 | Incineration method for saliferous organic mixed effluent |
-
2017
- 2017-05-15 CN CN201710338308.0A patent/CN108870413B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3946077A (en) * | 1973-03-28 | 1976-03-23 | Bayer Aktiengesellschaft | Process for oxidating hydrocarbons |
| CN1424535A (en) * | 2002-12-20 | 2003-06-18 | 巨化集团公司 | Combustion nozzle for cyelohexanone saponified waste water |
| CN101734824A (en) * | 2008-11-04 | 2010-06-16 | 王富绩 | Process for treating saponifiable waste alkali liquor by chemical method |
| CN102192513A (en) * | 2011-05-25 | 2011-09-21 | 大连科林能源工程技术开发有限公司 | Incinerator of multi-element multi-dimension chemical hazardous waste |
| CN102877351A (en) * | 2011-07-15 | 2013-01-16 | 中国石油化工集团公司 | Treatment method of high concentration waste alkali solution |
| CN103591591A (en) * | 2013-11-06 | 2014-02-19 | 武汉锅炉集团工程技术有限公司 | Saponification waste liquid combustion and alkali recovery boiler |
| CN103822216A (en) * | 2014-03-18 | 2014-05-28 | 江苏星瑞化工工程科技有限公司 | Incineration method for saliferous organic mixed effluent |
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