CN103555377B - A kind of de-benzene method of decompression - Google Patents
A kind of de-benzene method of decompression Download PDFInfo
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Abstract
The de-benzene method and apparatus of the open a kind of decompression of the present invention, the method adopts electrical heating method to replace traditional diamond heating method; Design a vertical debenzolizing tower simultaneously, in this debenzolizing tower, be designed to de-benzene section, RS Regenerator Section and storage tank section three sections from top to bottom, implement the de-benzene process of three body unifications; This equipment mainly comprises debenzolizing tower and connecting pipeline, it is characterized in that this de-benzene equipment only comprises a vertical debenzolizing tower, is followed successively by de-benzene section, RS Regenerator Section and storage tank section in this debenzolizing tower from top to bottom; Wherein de-benzene section is divided into rectifying section and stripping section, forms in rectifying section and stripping section by the tower tray of design quantity or filler; RS Regenerator Section is made up of the tower tray of design quantity; This de-benzene equipment also comprises de-benzene section electric heater and RS Regenerator Section electric heater; De-benzene section electric heater and RS Regenerator Section electric heater are installed in independently in operation room or in pump house.This de-benzene method and apparatus takes up an area few, and energy consumption saving wheel is little, and cost is low, and the benzene rate of recovery is high simultaneously, quality good.
Description
Technical field
The present invention relates to coking engineering projects crude benzol recovery technique, specifically the de-benzene method and apparatus of a kind of decompression.The method and equipment have energy-saving and emission-reduction advantage.
Background technology
Benzene is a kind of organic substance, has extensive use in the industry.At coking industry, the coke-oven gas generated in coal coking process is generally about 25-35g/Nm containing benzene
3, the benzene content after reclaiming is generally 0.4-0.6%.In order to recycle crude benzol better, by washing and absorption equipment, high boiling washing oil need be utilized as the benzene hydrocarbon in washing and absorption agent gas recovery, then rich oil distilled, obtain crude benzol.At present, the de-benzene process of most domestic mainly adopts the method for water at atmospheric pressure steam stripping, uses water vapor as thermal source.This processing method Problems existing mainly contains: 1, use a large amount of steam in production process, and generally often produce 1 ton of crude benzol consumption about 1.5 tons of steam, energy consumption is higher; 2, part aromatic hydrocarbon substance is inevitably dissolved owing to being blown into steam when overhead condensation becomes water of condensation, cannot technique reuse, directly discharge, the generation of waste water is comparatively large, contaminate environment, and Treatment of Coking Effluent is costly, and intractability is large; 3, the benzene rate of recovery is low, have impact on the yield of benzene, wastes the benzene raw materials of high-quality.
Chinese patent ZL200910014859.7 discloses a kind of negative pressure benzene removal method and apparatus.This processing method uses vacuum pump, makes debenzolizing tower and wash oil regenerator form negative-pressure operation, and debenzolizing tower adopts de-benzene tubular oven, washing oil regenerating column adopts regeneration tubular oven, carries out circulating-heating at the bottom of tower, provides thermal source to replace open steam for system.This technique eliminates the introducing of open steam owing to have employed negative-pressure operation, certain progress is had in energy-conserving and environment-protective, but still there is some deficiency following: 1, owing to introducing 2 equipment such as tubular oven and vacuum pump, increase cost of investment, add floor space, and the heat exchange efficiency of tubular oven is low, thermosteresis is large; 2, the furnace lining of tubular oven is short for work-ing life, and the too high circulating washing oil quality that makes of local temperature reduces, and easily coking occurs, and shortens the cycle of operation, clears up more difficult; 3, the use value of coke-oven gas is constantly developed in recent years, and price is also more and more higher, thus causes running cost constantly to increase; 4, the liquid measure due to debenzolizing tower rectifying section is little, not good to filling surface wetting effect, and theoretical stage efficiency is low, should not adopt structured packing; And stripping section adopts inclined hole tower tray, column plate thermo-efficiency is low, and working cost is high, and processing power is little, and Pressure Drop is large, easily blocks, is unfavorable for industrial practical application.
Chinese patent 201110085678.0 discloses the de-benzene distillation technique of a kind of decompression, it is compared with Chinese patent ZL200910014859.7, decrease the design of a tubular oven, save floor space, but it is because adopting tubular oven heating process, keep away unavoidably because of deficiency that tubular oven design is brought; Cancel the design of regenerator column, though reach the object of investment reduction, the situation that production capacity is comparatively large or follow-up Xi Ben workshop section is higher to benzene specification of quality in coking industry, its application is still subject to not little limitation.
Summary of the invention
In order to overcome the deficiencies in the prior art, the technical problem that quasi-solution of the present invention is determined is, provide a kind of decompression de-benzene method and apparatus, the method adopts electrical heating method to replace traditional diamond heating method; Meanwhile, main equipment debenzolizing tower is single tower, i.e. the technique of de-benzene section, RS Regenerator Section and the storage tank Duan Santi unification of design in debenzolizing tower; This equipment adopts electric heater unit, replaces traditional tubular oven completely, and design the unification of debenzolizing tower, regenerator column and storage tank tower three tower simultaneously, save floor space, improve effects of energy saving and emission reduction, reduce expense, the benzene rate of recovery is high simultaneously, quality good.
The technical scheme that the present invention solves described method and technology problem is, the de-benzene method of a kind of decompression of design, the method adopts electrically heated to provide thermal source for de-benzene process, designs a vertical debenzolizing tower simultaneously, is designed to three sections from top to bottom in this debenzolizing tower: de-benzene section, RS Regenerator Section and storage tank section; Its concrete technology step is as follows:
From the rich oil of Xi Ben workshop section after rich oil pump, enter in poor oil-rich heat exchanger, the oil-poor heat exchange of heat with carrying out storage tank section turning oil bottom autospasy benzene section and exporting, enters de-benzene section by rich oil import; De-benzene section top is carried out after condensation by crude benzol vapor outlet crude benzol vapour out through crude benzol condenser, enter crude benzol water-and-oil separator and carry out oily water separation, crude benzol after separation is by after crude benzol reflux pump, crude benzol is divided into two strands, one delivers to de-benzene section refluxing opening as trim the top of column, and another strand is sent into crude benzol storage tank and entered next workshop section; From a small amount of crude benzol of not condensing through crude benzol trap reclaims not condensing that crude benzol water-and-oil separator is discharged, the crude benzol after recovery returns crude benzol water-and-oil separator, and the residue of discharging from crude benzol trap not condensing is discharged by vacuum pump; Water treatment workshop section is delivered to through waste water pump from the isolated waste water of crude benzol water-and-oil separator; The rectifying section of de-benzene section, at the mode extraction naphtalene oil of naphtalene oil extraction mouth side take-off, is sent to naphtalene oil separating tank, then is pumped to naphtalene oil process workshop section by naphtalene oil after overcooling;
De-benzene section Base Heat is oil-poor sends into storage tank section by outside pipe arrangement, then exported by de-benzene section recycle pump extraction by storage tank section turning oil and be divided into two strands by certain design quantity, one is oil-poor with the heat exchange of raw material rich oil in poor oil-rich heat exchanger, then enters Xi Ben workshop section through oil-poor water cooler cooling; Another strand oil-poor, and by being further divided into two strands after de-benzene section electric heater heating, one returns de-benzene section as thermal source by taking off the import of benzene section turning oil, and another stock is delivered to oil-poor import and entered RS Regenerator Section and regenerate;
RS Regenerator Section top establishes spiral coil cooling tube to utilize recirculated cooling water to carry out condensing cooling as RS Regenerator Section inside from backflow to RS Regenerator Section top gas, is exported by RS Regenerator Section turning oil equally and utilize RS Regenerator Section recycle pump to be delivered to oil-poor bottom RS Regenerator Section the bottom being returned RS Regenerator Section after RS Regenerator Section electric heater heats by the import of RS Regenerator Section turning oil bottom RS Regenerator Section; Being back to resurgent gases return port from the resurgent gases outlet at RS Regenerator Section top with gas phase after major part regenerating wash oil enters bottom de-benzene section, as the thermal source of de-benzene section; The residual oil of RS Regenerator Section tower reactor sends to the large tank of tar through slag-drip opening, is incorporated to Process of Tar Processing.
The technical scheme that the present invention solves equipment and technology problem is, the de-benzene equipment of a kind of decompression of design, this equipment takes off benzene method according to electrically heated of the present invention, comprises debenzolizing tower, poor oil-rich heat exchanger, oil-poor water cooler, crude benzol condenser, crude benzol water-and-oil separator, crude benzol trap, naphtalene oil separating tank, rich oil pump, de-benzene section recycle pump, RS Regenerator Section recycle pump, waste water pump, naphtalene oil pump, vacuum pump, crude benzol reflux pump; Debenzolizing tower is provided with refluxing opening, rich oil import, de-benzene section turning oil import, naphtalene oil extraction mouth, resurgent gases return port, crude benzol vapor outlet, oil-poor import, resurgent gases outlet, the import of RS Regenerator Section turning oil, the outlet of RS Regenerator Section turning oil, slag-drip opening and the outlet of storage tank section turning oil; Also have by-pass valve control necessary on connecting pipeline and pipeline, measuring instrument and interconnecting piece, it is characterized in that: this de-benzene equipment only comprises a vertical debenzolizing tower, is divided into three sections from top to bottom in this debenzolizing tower, is followed successively by de-benzene section, RS Regenerator Section and storage tank section; Wherein de-benzene section is divided into rectifying section and stripping section, forms in rectifying section and stripping section by the tower tray of design quantity or filler; RS Regenerator Section is made up of the tower tray of design quantity; This de-benzene equipment also comprises de-benzene section electric heater and RS Regenerator Section electric heater; De-benzene section electric heater and RS Regenerator Section electric heater are installed in independently in operation room or in pump house.
Compared with prior art (the negative pressure benzene removal technique particularly described in patent ZL200910014859.7), the inventive method and equipment have following characteristics:
1, the heating system of tube furnace is eliminated, change electric heater heating system (as de-benzene section electric heater and RS Regenerator Section electric heater) into, ensure that stability and the homogeneity of heat supply, thermo-efficiency improves 25-30%, washing oil is coking not easily, washing oil quality comparatively diamond heating mode will be got well, and on-the-spot without combustion emission, overall energy consumption is low than the patent ZL200910014859.7 negative pressure benzene removal technique of same scale;
2, negative pressure benzene removal process only utilizes the high-temperature hot of debenzolizing tower still oil-poor as thermal source, does not use open steam.So both ensure the efficiency utilization of the energy, avoid energy dissipation, additionally reduce the waste water because steam produces simultaneously, there is energy-saving and emission-reduction effect significantly, be conducive to environmental protection;
3, vacuum pump is established at tower top place, can the negative pressure requirements of guarantee section important system.Subnormal ambient is conducive to the boiling point reducing benzene, improve the relative volatility of benzene in Components of Wash Oil and the temperature of reduction tower top effusion mixed vapour, operating reflux ratio can be made to reduce, be convenient to separation and the condensation of crude benzol, there is certain energy-saving effect, effectively be down to less than 0.15% by oil-poor containing benzene, the yield of benzene to dry coal compared with prior art improves more than 35%, is far superior to prior art;
4, conventional atmospheric technique needs to arrange multiple water-and-oil separator; And present invention process is negative-pressure operation, owing to not having steam to introduce, thus crude benzol Separation of Water comparatively atmospheric processes is a lot of less, only need a crude benzol return tank just can meet the static separation requirement of crude benzol Separation of Water, technique is simple.
Accompanying drawing explanation
Fig. 1 is that the present invention is reduced pressure the process flow diagram of a kind of embodiment of de-benzene method and apparatus.
Fig. 2 is that the present invention is reduced pressure the vertical debenzolizing tower structural representation of main equipment of a kind of embodiment of de-benzene method and apparatus.In figure, vertical debenzolizing tower is divided into three sections, is followed successively by de-benzene section, RS Regenerator Section and storage tank section from top to bottom.
Embodiment
The present invention is described further below in conjunction with embodiment and accompanying drawing thereof.Specific embodiment, only for describing the application in detail, does not limit the protection domain of the application's claim.
The decompression of the present invention's design takes off benzene method (abbreviation method, see Fig. 1,2) on traditional de-benzene process basis, electrical heating method is innovatively adopted to provide thermal source for de-benzene process, therefore can be described as electrically heated and take off benzene method, design the unification of debenzolizing tower, regenerator column and storage tank tower three tower for vertical debenzolizing tower simultaneously, in this debenzolizing tower, be designed to three sections from top to bottom: de-benzene section, RS Regenerator Section and storage tank section; De-benzene section is divided into rectifying section and stripping section, forms in rectifying section and stripping section by the tower tray of design quantity or filler; RS Regenerator Section is made up of the tower tray of design quantity; Also comprise de-benzene section electric heater and RS Regenerator Section electric heater; The concrete technology that electrically heated takes off benzene method is:
From the rich oil of Xi Ben workshop section, temperature is 25-30 DEG C, after rich oil pump 8, enter in poor oil-rich heat exchanger 2, with carry out heat oil-poor (temperature the is 200-210 DEG C) heat exchange that storage tank section turning oil bottom autospasy benzene section 101 exports 1031, the rich oil temperature after heat exchange is increased to 170-175 DEG C, is entered the de-benzene section 101 of debenzolizing tower 1 by rich oil import 1012, de-benzene section 101 head temperature controls at 55-60 DEG C, and pressure-controlling is in 30-35KPa(absolute pressure); De-benzene section 101 top by crude benzol vapor outlet 1016 crude benzol vapour out after crude benzol condenser 4 carries out condensation, enter crude benzol water-and-oil separator 5 and carry out oily water separation, crude benzol, by after crude benzol reflux pump 14, is divided on two strands (roads): one delivers to de-benzene section refluxing opening 1011 as trim the top of column by the crude benzol after separation; Another strand is sent into crude benzol storage tank and is entered next workshop section; From the not condensing that crude benzol water-and-oil separator 5 is discharged, a small amount of crude benzol in crude benzol trap 6 reclaims not condensing, crude benzol after recovery returns crude benzol water-and-oil separator 5, from crude benzol trap 6 discharge residue not condensing discharged by vacuum pump 13, make de-benzene section 101 top pressure meet the requirement of design load, namely meet pressure-controlling in 30-35KPa(absolute pressure) requirement; Water treatment workshop section is delivered to through waste water pump 11 from the isolated waste water of crude benzol water-and-oil separator 5; The rectifying section 101a of de-benzene section 101, at the mode extraction naphtalene oil of naphtalene oil extraction mouth 1014 with side take-off, is sent to naphtalene oil separating tank 7, then delivers to naphtalene oil process workshop section by naphtalene oil pump 12 after overcooling.
De-benzene section 101 bottom temp controls at 200-210 DEG C, pressure-controlling is in 45-50kPa(absolute pressure), de-benzene section 101 Base Heat is oil-poor sends into storage tank section 103 by outside pipe arrangement, then export 1031 by storage tank section 103 turning oil draw by de-benzene section recycle pump 9 and be divided into two strands by certain design quantity: one is oil-poor with the heat exchange of raw material rich oil in poor oil-rich heat exchanger 2, then enters Xi Ben workshop section through oil-poor water cooler 3 cooling; Another strand oil-poor be heated to 220-230 DEG C by de-benzene section 101 electric heater 15 after, be further divided into two strands, one returns de-benzene section as thermal source by taking off benzene section turning oil import 1013, and another stock (being about the 1-1.5% of oil-poor amount total mass) is delivered to oil-poor import 1021 and entered RS Regenerator Section 102 and regenerate.
RS Regenerator Section 102 head temperature control 230-235 DEG C, pressure-controlling is in 55-65kPa(absolute pressure); RS Regenerator Section 102 bottom temp controls at 260-270 DEG C, pressure-controlling is in 65-70kPa(absolute pressure), spiral coil cooling tube 1026 is established at RS Regenerator Section 102 top, recirculated cooling water is utilized to carry out condensing cooling to RS Regenerator Section top gas, inner from backflow as RS Regenerator Section 102, same bottom RS Regenerator Section 102, exporting 1024 by RS Regenerator Section turning oil utilizes RS Regenerator Section recycle pump 10 to be delivered to after RS Regenerator Section electric heater 16 is heated to 280-290 DEG C by oil-poor bottom RS Regenerator Section 102, is returned to the bottom of RS Regenerator Section 102 by RS Regenerator Section turning oil import 1023; After major part regenerating wash oil, be back to resurgent gases return port 1015 from the resurgent gases outlet 1022 at RS Regenerator Section 102 top with gas phase, enter bottom de-benzene section 101, as the thermal source of de-benzene section 101; The residual oil of RS Regenerator Section 102 tower reactor sends to the large tank of tar through slag-drip opening 1025, is incorporated to Process of Tar Processing.
The inventive method is a kind of electrically heated decompression de-benzene process, and it replaces water vapour process furnace or tubular oven in prior art, as the main source of the energy in present invention process with described electric heater unit.
The present invention devises the de-benzene equipment of decompression simultaneously and (is called for short equipment, see Fig. 2), this equipment takes off benzene method according to electrically heated of the present invention, comprises main equipment debenzolizing tower 1, poor oil-rich heat exchanger 2, oil-poor water cooler 3, crude benzol condenser 4, crude benzol water-and-oil separator 5, crude benzol trap 6, naphtalene oil separating tank 7, rich oil pump 8, de-benzene section recycle pump 9, RS Regenerator Section recycle pump 10, waste water pump 11, naphtalene oil pump 12, vacuum pump 13 and crude benzol reflux pump 14; Debenzolizing tower is provided with refluxing opening 1011, rich oil import 1012, de-benzene section turning oil import 1013, naphtalene oil extraction mouth 1014, resurgent gases return port 1015, crude benzol vapor outlet 1016, oil-poor import 1021, resurgent gases outlet 1022, RS Regenerator Section turning oil import 1023, RS Regenerator Section turning oil outlet 1024, slag-drip opening 1025, storage tank section turning oil outlet 1031, also has the component such as by-pass valve control necessary on connecting pipeline and pipeline, measuring instrument and interconnecting piece; It is characterized in that: this de-benzene equipment only comprises a vertical debenzolizing tower 1, is divided into three sections from top to bottom in this debenzolizing tower 1, is followed successively by de-benzene section 101, RS Regenerator Section 102 and storage tank section 103; Wherein be divided into rectifying section 101a and stripping section 101b in de-benzene section 101, form by the tower tray of design quantity or filler in rectifying section 101a and stripping section 101b; Establish 13 layers of CJST tower tray 1017 in the rectifying section 101a of embodiment, stripping section 101b is two sections of structured packings 1019, and filler top adopts between tank type liquid distributor 1018, two sections of structured packings 1019 and adopts Box-type Gas-liquid Distributor 1020; RS Regenerator Section 102 adopts 5 layers of CJMP tower tray 1027; RS Regenerator Section is made up of the tower tray of design quantity; In RS Regenerator Section, embodiment adopts CJMP tower tray, and its top is provided with spiral coil cooling tube 1026; This de-benzene equipment also comprises de-benzene section electric heater 15 and RS Regenerator Section electric heater 16, is to ensure use safety, and de-benzene section electric heater is arranged on system within battery limit independently in operation room or be placed in pump house; In like manner, RS Regenerator Section electric heater is also arranged on system within battery limit independently in operation room or be placed in pump house.
The electric heater that the inventive method and equipment adopt, commercially directly can buy according to power requirement and obtain.What the electric heater selected in the present embodiment adopted is electrothermal tube direet-heating type, has multiple power selection button, carries out power selection, electric heater has temperature adjustment buttons according to throughput, carry out temperature adjustment according to operational condition; Electrothermal tube runs into damage, can directly change, easy access, convenient disassembly; In addition, when throughput is not high, also can closes regenerator column electric heater, avoid production capacity surplus, cause waste.
Described de-benzene section electric heater 15 inside and RS Regenerator Section electric heater 16 inside are all designed with power device, as electrothermal tube etc.
As preferably, the rectifying section tower tray of de-benzene section adopt this tower tray of radial side pilot jet tray CJST(be applicant in first patent, i.e. " a kind of radial side pilot jet tray ", the radial side pilot jet tray of claim 1 defined in patent No. ZL200620025314.8), this tower tray has the advantages such as throughput is large, tray efficiency is high, pressure reduces, turndown ratio is large; The stripping section of de-benzene section preferentially adopts the structured packing of 250Y type and the tank type liquid distributor matched and Box-type Gas-liquid Distributor; RS Regenerator Section adopt the CJMP tower tray of certain design quantity (this tower tray be applicant in first patent, i.e. " a kind of film spray no-back mixing column plate ", the film spray no-back mixing column plate of claim 1 defined in patent No. ZL200910067917.2), compared with other column plates, this column plate has that treatment capacity is large, anti-clogging is strong, plate efficiency high, gas liquid interfacial area can be increased, improve regeneration effect, in RS Regenerator Section, CJMP tower tray top is provided with spiral coil cooling tube.
The technological principle of the inventive method is: rely on low-voltage operating conditions, reduce rich oil boiling point (boiling point away under rich oil normal pressure), and improve the relative volatility of benzene class material, under the condition lower than atmospheric operation temperature, benzene class material is steamed from rich oil de-, rich oil is regenerated.
The inventive method and equipment are compared with the innovation of other negative pressure benzene removal technical process, de-benzene section adopts de-benzene section electric heater, RS Regenerator Section adopts RS Regenerator Section electric heater as the heat source of main equipment debenzolizing tower in the inventive method, replaces traditional gas pipe type furnace heating system; The three body unification of de-benzene section, RS Regenerator Section and storage tank, saves floor space, and has enough height, be conducive to tower reactor fluid-tight.
Owing to being decompression operation, needing enough height bottom de-benzene section, be conducive to fluid-tight bottom de-benzene section, and the potential energy that potential difference can be utilized to produce makes oil-poorly bottom de-benzene section can certainly flow to storage tank section.The method and equipment, have that the benzene rate of recovery is high, quality good; Investment is with working cost is low, floor space is little; The features such as thermo-efficiency is high, energy-conserving and environment-protective, are particularly useful for the producer that coal gas has higher utility value or electric power resource to enrich, as having the relevant enterprise application of coal gas methyl alcohol workshop section or power station.
The sharpest edges of the inventive method are energy-saving and emission-reduction, and cleaner production is free from environmental pollution, is in particular in: the thermo-efficiency of electric heater is up to more than 95%, on-the-spot without combustion emission;
The Economic and Efficiency Analysis of the inventive method: with coking production ability 1,000,000 tons/year, rich oil amount is 100t/h is example, and the energy consumption comparison per hour of three kinds of methods refers to table 1.
Table 1 various de-benzene process energy consumption performance analysis table
As can be seen from the data of table 1, two kinds of negative pressure benzene removal technique comparatively atmospheric processes all saves steam consumption, reduces energy consumption, decreases discharge of wastewater, saved the expense of wastewater treatment; Simultaneously owing to reducing the temperature of exhaust gas under the environment of negative-pressure operation, therefore decrease the consumption of water coolant.
In two kinds of negative pressure benzene removal technique, negative pressure benzene removal electrical heating process method of the present invention, compared with the negative pressure benzene removal tube furnace processing method of prior art, does not have combustion emission, is the first-selected processing method realizing energy-saving, emission-reducing, environment friendly target.
In sum, be followed successively by through calculating three kinds of process operation costs: once-through pipe still technique > negative pressure benzene removal tube furnace technique > negative pressure benzene removal electrical heating process.
The present invention does not address part and is applicable to prior art.
Claims (1)
1. the de-benzene method of decompression, the method adopts electrically heated to provide thermal source for de-benzene process, designs a vertical debenzolizing tower simultaneously, is designed to three sections from top to bottom in this debenzolizing tower: de-benzene section, RS Regenerator Section and storage tank section;
Its concrete technology step is as follows:
From the rich oil of Xi Ben workshop section, temperature is 25-30 DEG C, after rich oil pump, enter in poor oil-rich heat exchanger, with the oil-poor heat exchange of heat carrying out storage tank section turning oil bottom autospasy benzene section and export, the rich oil temperature after heat exchange is increased to 170-175 DEG C, enters de-benzene section by rich oil import; De-benzene section head temperature controls at 55-60 DEG C, pressure-controlling is at 30-35KPa, de-benzene section top is carried out after condensation by crude benzol vapor outlet crude benzol vapour out through crude benzol condenser, enter crude benzol water-and-oil separator and carry out oily water separation, crude benzol after separation is by after crude benzol reflux pump, crude benzol is divided into two strands, one delivers to de-benzene section refluxing opening as trim the top of column, and another strand is sent into crude benzol storage tank and entered next workshop section; From a small amount of crude benzol of not condensing through crude benzol trap reclaims not condensing that crude benzol water-and-oil separator is discharged, crude benzol after recovery returns crude benzol water-and-oil separator, from crude benzol trap discharge residue not condensing discharged by vacuum pump, make de-benzene section top pressure control at 30-35KPa; Water treatment workshop section is delivered to through waste water pump from the isolated waste water of crude benzol water-and-oil separator; The rectifying section of de-benzene section, at the mode extraction naphtalene oil of naphtalene oil extraction mouth side take-off, is sent to naphtalene oil separating tank, then is pumped to naphtalene oil process workshop section by naphtalene oil after overcooling;
De-benzene section (101) bottom temp controls at 200-210 DEG C, pressure-controlling is at 45-50kPa, de-benzene section Base Heat is oil-poor sends into storage tank section by outside pipe arrangement, then exported by de-benzene section recycle pump extraction by storage tank section turning oil and be divided into two strands by certain design quantity, one is oil-poor with the heat exchange of raw material rich oil in poor oil-rich heat exchanger, then enters Xi Ben workshop section through oil-poor water cooler cooling; Another burst of oil-poor passing through is further divided into two strands after de-benzene section (101) electric heater (15) is heated to 220-230 DEG C, one returns de-benzene section as thermal source by taking off the import of benzene section turning oil, and another stock is delivered to oil-poor import and entered RS Regenerator Section and regenerate;
RS Regenerator Section head temperature control 230-235 DEG C, pressure-controlling is at 55-65kPa, RS Regenerator Section bottom temp controls at 260-270 DEG C, pressure-controlling is at 65-70kPa, RS Regenerator Section top establishes spiral coil cooling tube to utilize recirculated cooling water to carry out condensing cooling to RS Regenerator Section top gas, as RS Regenerator Section inside from backflow, exported by RS Regenerator Section turning oil equally bottom RS Regenerator Section and utilize RS Regenerator Section recycle pump to be delivered to oil-poor bottom RS Regenerator Section the bottom being returned RS Regenerator Section after RS Regenerator Section electric heater is heated to 280-290 DEG C by the import of RS Regenerator Section turning oil; Being back to resurgent gases return port from the resurgent gases outlet at RS Regenerator Section top with gas phase after major part regenerating wash oil enters bottom de-benzene section, as the thermal source of de-benzene section; The residual oil of RS Regenerator Section tower reactor sends to the large tank of tar through slag-drip opening, is incorporated to Process of Tar Processing;
Above-mentioned mentioned pressure all refers to absolute pressure.
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103801099A (en) * | 2014-02-26 | 2014-05-21 | 北京首钢国际工程技术有限公司 | Negative-pressure distillation process system for integrated debenzolization and regeneration tower |
| CN104312638B (en) * | 2014-10-30 | 2016-04-13 | 济南冶金化工设备有限公司 | Thermal coupling negative pressure benzene removal, regeneration integrated apparatus |
| CN104910972B (en) * | 2015-06-26 | 2017-10-27 | 山东钢铁股份有限公司 | A kind of rich oil de-benzene system for handling coke-stove gas |
| CN104927929A (en) * | 2015-06-29 | 2015-09-23 | 济南冶金化工设备有限公司 | Crude benzene distilling and washing oil regenerating heating system and method |
| CN108096999B (en) * | 2017-12-22 | 2023-06-20 | 中冶焦耐(大连)工程技术有限公司 | Reboiler method negative pressure crude benzene distillation process |
| CN107890684B (en) * | 2017-12-22 | 2023-06-16 | 中冶焦耐(大连)工程技术有限公司 | Reboiler method negative pressure crude benzol distillation system |
| CN108424793A (en) * | 2018-05-17 | 2018-08-21 | 山东焦化技术咨询服务有限公司 | Rich oil de-benzene system and rich oil de-benzene method |
| CN111253203A (en) * | 2020-03-17 | 2020-06-09 | 本钢板材股份有限公司 | Heat exchange optimization process for crude benzene distillation section |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2915212Y (en) * | 2006-02-08 | 2007-06-27 | 天津市创举科技有限公司 | A radial side pilot jet tray |
| CN101507883A (en) * | 2009-02-23 | 2009-08-19 | 天津市创举科技有限公司 | Film spray no-back mixing column plate |
| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN101993736A (en) * | 2009-08-14 | 2011-03-30 | 鞍钢集团工程技术有限公司 | Method and device for regenerating circular wash oil during rich oil debenzolization of gas purification |
-
2013
- 2013-10-24 CN CN201310507035.XA patent/CN103555377B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2915212Y (en) * | 2006-02-08 | 2007-06-27 | 天津市创举科技有限公司 | A radial side pilot jet tray |
| CN101507883A (en) * | 2009-02-23 | 2009-08-19 | 天津市创举科技有限公司 | Film spray no-back mixing column plate |
| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN101993736A (en) * | 2009-08-14 | 2011-03-30 | 鞍钢集团工程技术有限公司 | Method and device for regenerating circular wash oil during rich oil debenzolization of gas purification |
Non-Patent Citations (1)
| Title |
|---|
| 脱苯塔采萘及脱苯工艺改进的探讨;商恩霞等;《化学工程》;20110131;第39卷(第1期);第91页第1栏第2段 * |
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Address after: 300130 the Binhai New Area of Tianjin Huayuan Industrial Zone (outer ring) Hai Tai innovation six road No. 2 15-1 Patentee after: Tianjin pioneering Polytron Technologies Inc Address before: 300130 East Hospital, Hebei University of Technology, 8 glorious road, Hongqiao, Tianjin Patentee before: Tianjin Chuangju Science and Technology Co., Ltd. |