CN102464546B - Double-tower depropanization process for reducing reboiler scaling - Google Patents
Double-tower depropanization process for reducing reboiler scaling Download PDFInfo
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Abstract
The invention relates to a double-tower depropanization process for reducing reboiler scaling. The double-tower depropanization process for reducing reboiler scaling comprises the steps: a feed gas enters a high pressure depropanization tower after being compressed at I-IV sections and subjected to alkali wash and drying; C3 and ingredients above C3 in a high pressure depropanization tower kittle enter a low pressure depropanization tower; one part of C3 and ingredients under C3 at the top of the high pressure depropanization tower returns to the high pressure depropanization tower; and one part of material at the top of the low pressure depropanization tower returns to the high pressure depropanization tower, wherein the pressure of the high pressure depropanization tower is 1.3-1.5MPa, the mole percentage of the C3 ingredient in the tower kettle to the total C3 ingredient entering the high pressure depropanization tower is 25-45%, and the tower kettle temperature is controlled within 70-80 DEG C. According to the process provided by the invention, scaling and tower plate blocking of the reboiler are reduced greatly, and the service life of the equipment is prolonged.
Description
Technical field
The present invention relates to a kind of depropanizing technique, particularly relate to a kind of for reducing the high-low pressure tower depropanizing technique of reboiler fouling, column plate obstruction.
Background technology
In ethylene cracking gas separation process, a large amount of C4 that contain in depropanizing tower tower reactor material and above unsaturated hydrocarbons thereof, it very easily generates polymkeric substance under comparatively high temps, causes reboiler fouling, column plate to stop up.
In early stage separation process, mostly adopt single tower process, i.e. low pressure depropanizing tower.But, reduce depropanizing tower working pressure to reduce tower reactor temperature, when solving reboiler and tower bottom because of polymkeric substance generation fouling and blockage problem, its tower top temperature is corresponding reduction also, and the freezing power consumption of propylene of condenser is increased thereupon.
More employing Technical analysis technical process in recent years, has slowed down polymer buildup to a certain extent.Technical analysis feature is: be divided into high pressure depropanizer and low pressure depropanizing tower, high-pressure tower carries out the non-clear cutting of C3, and tower reactor contains part C3, makes tower reactor material component lighter, reduces tower reactor temperature.High pressure materials at bottom of tower C3 and C4+ enter lower pressure column, further C3 are separated with C4.But in actual production, high pressure depropanizer still temperature is still higher, and more than 80 DEG C, scale problems is still more outstanding conventionally, and the operation of equipment cycle is shorter.
The main component of foulant is the cinnamic multipolymer of divinyl and part, wherein contains a small amount of hydrocarbon oxide.What harm was maximum is butadiene-based polymer, will increase as core exponentially once generate.More generally acknowledged butadiene polymerization mechanism now, divinyl reacts with intrasystem oxygen, generates the superoxide of divinyl.The superoxide one of divinyl is to make the rapid autohemagglutination of divinyl as a kind of autohemagglutination catalyzer; Another kind may be the superoxide of divinyl under the existence of water and iron ion, Butadiene Peroxide is decomposed and produces free radical, these free radicals further increase, and form the polymkeric substance of divinyl.
Temperature is the important factor of bringing out divinyl autohemagglutination in depropanizing tower, and its speed of response raises with temperature and sharply accelerates, so strict red-tape operati temperature is the very important measure that slows down divinyl autohemagglutination and reduce fouling.
For assurance device long-period stable operation, the measures such as the solid impurity content (as siccative powder) in industrial common employing Optimization of Ethylene cracking stock, the processing condition of optimizing depropanization system, suppression equipment corrosion and control material.The technical measures that current each ethylene production producer generally adopts are to select high-efficiency polymerization inhibitor to suppress the fouling of depropanization system.Most of devices all adopt the stopper that simultaneously injects proper concn in depropanizing tower charging and reboiler ingress, and tower reactor temperature is controlled in 80 DEG C.The consumption of stopper is determined according to its performance and raw material, technique and device situation.The stopper consumption of domestic each ethylene unit depropanizing tower differs greatly.Need to carry out necessary evaluation for concrete raw material and technique in advance, operator must monitor that whether the work of stopper note robot system is normal constantly.In production, usually run into because the fault of stopper pump causes injection rate and reduce the situation that note is not entered even completely.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of high-low pressure tower depropanizing technique that reduces reboiler fouling, column plate obstruction.
A kind of Technical analysis technique that reduces reboiler fouling of the present invention, described double tower comprises high pressure depropanizer and low pressure depropanizing tower, compressor is provided with the compression of I-V section altogether, every intersegmental intersegmental separating tank that is provided with, unstripped gas is after the compression of I-IV section, enter high pressure depropanizer through alkali cleaning with after being dried, the above component of the C3 of high pressure depropanizer tower reactor and C3 enters low pressure depropanizing tower, the following component part of high pressure depropanizer tower top C3 and C3 is returned to high pressure depropanizer, another part is sent to upstream device processing, a low pressure depropanizing tower tower top material part is returned to high pressure depropanizer, another part is sent to downstream unit processing, the pressure of high pressure depropanizer is 1.3-1.5MPa, in this high pressure depropanizer tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 25-45% to C3 component, tower reactor temperature is controlled at 70-80 DEG C.
A kind of Technical analysis technique that reduces reboiler fouling of the present invention, wherein the pressure of preferred described high pressure depropanizing is 1.3-1.4MPa, tower reactor temperature is 70-75 DEG C, and in tower reactor, C3 component accounts for the molecular fraction 30-45% of the total C3 component that enters high pressure depropanizer.
A kind of Technical analysis technique that reduces reboiler fouling of the present invention, wherein said unstripped gas is the unstripped gas that oil obtains after pyrolyzer cracking, described low pressure depropanizing tower tower top material is C3 component, this low pressure depropanizing tower tower reactor composition is the above component of C4 and C4, send to downstream unit processing, the working pressure 0.8-1.0MPa of this low pressure depropanizing tower is the conventional numerical value in this area.
A kind of Technical analysis technique that reduces reboiler fouling of the present invention, wherein also comprise IV, the intersegmental separating tank of V bottom component are entered to lighter hydrocarbons stripping tower and isolate C3 and following component and C3 and above component, C3 and above component enter low pressure depropanizing tower, isolate C3 component, C4 and above component, C3 component is low pressure depropanizing tower tower top material, a part is returned to the tower reactor of high pressure depropanizer, supplement the content of C3 component in high pressure depropanizer tower reactor, a part is sent to downstream unit processing, and C4 and above component are this low pressure depropanizing tower tower reactor compositions.Technique of the present invention returns to high pressure depropanizer by a control high pressure depropanizer tower top C3 component part and a low pressure depropanizing tower tower top C3 component part is returned to these two return wires of high pressure depropanizer, the molecular fraction that makes the content of C3 component in high-pressure tower tower reactor account for the total C3 component that enters high pressure depropanizer is 25-45%, makes tower reactor temperature be controlled at 70-80 DEG C.
Wherein, unstripped gas enters in separating tank after alkali cleaning, isolates light hydrocarbon gas component and heavy hydrocarbon liquid component, and the heavy hydrocarbon liquid component obtaining at the bottom of tank enters lighter hydrocarbons stripping tower and isolates C3 and following component and C3 and above component.The isolated C3 of lighter hydrocarbons stripping tower and following component are returned to the intersegmental separating tank of III, IV.
Technique of the present invention is by reducing the pressure ratio of cracking gas compressor IV section, increase the pressure ratio of V section, make the working pressure of high pressure depropanizer remain on 1.3～1.5MPaA, tower reactor temperature is controlled at 70-80 DEG C, the inlet pressure of wherein said compression V section is 1.3-1.5MPa, and the top hole pressure of compression V section is 2.6-3.0 with the ratio of inlet pressure; The top hole pressure of described compression IV is 1.8-2.0 with the ratio of inlet pressure, and the top hole pressure scope of compression IV is 1.6-1.8MPa.
A kind of Technical analysis technique that reduces reboiler fouling of the present invention, by reducing the pressure ratio of cracking gas compressor IV section, increase the pressure ratio of V section, make the working pressure of high pressure depropanizer remain on 1.3～1.5MPaA, less than conventional working pressure (generally more than 1.6MPa), be conducive to reduce the temperature of tower reactor; Low pressure depropanizing tower top arranges a return wire of going to high pressure depropanizer, in this return wire, material is C3 component, by being back to high pressure depropanizer, can play the effect of dilution high pressure depropanizer still material, reduce the content of C4 component, increase the content of C3 component, and then reduce tower reactor temperature.In addition, lighter hydrocarbons stripping tower also can be set in technique, for C3 and the above heavy constituent of IV, the intersegmental separating tank of V bottom component are separated in advance, comprising most of C4 unsaturated hydrocarbons, these heavy constituents directly enter low pressure depropanizing tower, stride across high pressure depropanizer, because C4 unsaturated hydrocarbons content in high pressure depropanizer charging reduces, tower reactor temperature can decline, and can reduce tower reactor fouling.Technique of the present invention by aforesaid method by the pressure-controlling of high pressure depropanizer at 1.3-1.5MPa, in tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 25-45% to the content of C3 component, tower reactor temperature is controlled at 70-80 DEG C, greatly reduce or avoided the fouling of reboiler and column plate to stop up, having extended the work-ing life of equipment.
Brief description of the drawings
Fig. 1 is the Technical analysis process flow diagram that the present invention reduces reboiler fouling;
Fig. 2 is another embodiment schematic flow sheet of Technical analysis technique that the present invention reduces reboiler fouling.
Description of reference numerals: 1-high pressure depropanizer; 2-low pressure depropanizing tower; 3-lighter hydrocarbons stripping tower; 13,14,15,16,4-compressor I to V section; 17-I section entrance separating tank; 18,19,20, the intersegmental separating tank of 21-; 25,26,27,28-intersegmental cooler; 22-soda-wash tower; 23-dryer feed separating tank; 24-gas flow dryer; 6-carbon two hydrogenators; 7-carbon two hydrogenator outlet water coolers; 8-high pressure depropanizer separating tank; 9-low pressure depropanizing tower condenser; 10-low pressure depropanizing tower separating tank; 29-lime set pump; 30-petrol-feed pump; 31-alkali cleaning tower top water cooler; 32-liquid phase moisture eliminator.
Embodiment
Below in conjunction with drawings and Examples, technical characterictic and the advantage with other above-mentioned to the present invention are described in more detail.
Embodiment 1
As shown in Figure 1, a kind of Technical analysis technique that reduces reboiler fouling of the present invention, described double tower comprises high pressure depropanizer and low pressure depropanizing tower, compressor is provided with the compression of I-V section altogether, every intersegmental intersegmental separating tank that is provided with, the splitting gas obtaining from upstream equipment is after I section entrance separating tank 17 separates, gas enters compressor I to IV section 13, 14, 15, 16 compression and intersegmental separating tanks 18, 19, 20, 21 separate, the light hydrocarbon gas component that tank deck separates enters soda-wash tower 22 and removes carbonic acid gas, the sour gas such as sulfurous gas, soda-wash tower 22 top gas enter 23 gas-liquid separations of dryer feed separating tank after alkali cleaning tower top water cooler 31 is cooling.Dryer feed separating tank 23 top gas enter high pressure depropanizer 1 after gas flow dryer 24 is dry, and bottom liquid phases enters high pressure depropanizer 1 after liquid phase moisture eliminator 32 is dry;
In high pressure depropanizer 1, carry out the non-clear cutting of C3, be that tower top obtains C3 and following component, tower reactor contains C4 and above component and part C3, the component of tower top is carried out the hydrogenation reaction of carbon two unsaturated hydrocarbons after the compression of V section in carbon two hydrogenators 6, the product obtaining is after outlet water cooler 7 is cooling, in separating tank 8, isolate carbon two and following light hydrocarbon component and C3 component, carbon two and the following light hydrocarbon component of tank deck enter upstream device, at the bottom of tank, a C3 component part is delivered to upstream device processing, and a part is back to high pressure depropanizer 1 as refluxing;
At the bottom of low pressure depropanizing tower 2 towers, isolated C4 and above component are sent to downstream unit processing, the C3 component that tower top obtains enters separating tank 10 after condenser 9 condensations, an isolated C3 component part is delivered to downstream unit processing, a part is as the backflow of low pressure depropanizing tower, another part is as the return wire that is back to high pressure depropanizer 1, this return wire can inject the top of high pressure depropanizer, also can inject bottom, and object is to make tower reactor material component lighter;
In the embodiment of the present invention, after high pressure depropanizer 1 quantity of reflux regulates, in high pressure depropanizer 1 tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 25% to C3 component, tower reactor temperature is 79.7 DEG C, also can control molecular fraction that C3 component accounts for the total C3 component that enters high pressure depropanizer and be 30%, 35% or 45% is numerical value arbitrarily between 25%-45%, in the time being 45%, tower reactor temperature is 69.9 DEG C, for conventional charging situation, carry out condition calculating as shown in table 1:
The content of C3 component and tower reactor temperature in table 1 tower reactor
Compressor IV section top hole pressure is 1.8 with the ratio of inlet pressure, and top hole pressure is 1.6MPa, less than conventional top hole pressure and ratio, and IV inlet pressure value is with conventional consistent; V section top hole pressure is 2.6 with the ratio of inlet pressure, and inlet pressure is 1.4MPa, and V section top hole pressure is with conventional consistent; The working pressure of high pressure depropanizer is 1.4MPa; The working pressure of low pressure depropanizing tower is 0.8MPa, is this area routine operation numerical value.
Embodiment 2
As shown in Figure 2, a kind of Technical analysis technique that reduces reboiler fouling of the present invention, the splitting gas obtaining from upstream equipment is after I section entrance separating tank 17 separates, gas enters 13,14,15,16 compressions of compressor I to IV section and separates with intersegmental separating tank 18,19,20,21, the light hydrocarbon gas component that tank deck separates enters soda-wash tower 22 and removes the sour gas such as carbonic acid gas, sulfurous gas, and soda-wash tower 22 top gas enter 23 gas-liquid separations of dryer feed separating tank after alkali cleaning tower top water cooler 31 is cooling.Dryer feed separating tank 23 top gas enter high pressure depropanizer 1 after gas flow dryer 24 is dry, bottom liquid phases and IV, the intersegmental separating tank 21 bottom heavy hydrocarbon components of V enter lighter hydrocarbons stripping tower 3, isolate C3 and following light constituent and C3 and above heavy constituent, tower top light constituent returns to the intersegmental separating tank of III, IV, and at the bottom of tower, heavy constituent enters low pressure depropanizing tower 2 after liquid phase moisture eliminator 32 is dry;
In high pressure depropanizer 1, carry out the non-clear cutting of C3, be that tower top obtains C3 and following component, tower reactor contains C4 and above component and part C3, the component of tower top is carried out the hydrogenation reaction of carbon two unsaturated hydrocarbons after the compression of V section in carbon two hydrogenators 6, the product obtaining is after outlet water cooler 7 is cooling, in separating tank 8, isolate carbon two and following light hydrocarbon component and C3 component, carbon two and the following light hydrocarbon component of tank deck enter upstream device, at the bottom of tank, a C3 component part is delivered to upstream device, and a part is back to high pressure depropanizer 1 as refluxing;
At the bottom of low pressure depropanizing tower 2 towers, isolated C4 and above component are sent to downstream unit processing, the C3 component that tower top obtains enters separating tank 10 after condenser 9 condensations, an isolated C3 component part is delivered to downstream unit processing, a part is as the backflow of low pressure depropanizing tower, another part is as the return wire that is back to high pressure depropanizer 1, this return wire can inject the top of high pressure depropanizer, also can inject bottom, and object is to make tower reactor material component lighter;
In the embodiment of the present invention, after high pressure depropanizer 1 quantity of reflux regulates, in high pressure depropanizer 1 tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 45% to C3 component, and tower reactor temperature is 69.9 DEG C,
Compressor IV section top hole pressure is 2.0 with the ratio of inlet pressure, and top hole pressure is 1.8MPa, less than conventional top hole pressure and ratio, and IV inlet pressure value is with conventional consistent; V section top hole pressure is 3.0 with the ratio of inlet pressure, and inlet pressure is 1.5MPa, and V section top hole pressure is with conventional consistent; The working pressure of high pressure depropanizer is 1.5MPa; The working pressure of low pressure depropanizing tower is 1.0MPa, is this area routine operation numerical value.
The heavy hydrocarbon component obtaining at the bottom of III, the intersegmental separating tank 20 of IV and II, intersegmental separating tank 19 tanks of III is back to the intersegmental separating tank 18 of I, II, the raw gasline component part that the intersegmental separating tank 18 of I, II obtains is depressed into upstream equipment processing with petrol-feed pump 30, another part is back to I section entrance separating tank 17, and the water-setting liquid that 17 ends of I section entrance separating tank obtain is delivered to upstream equipment processing through lime set pump 29.
The present invention is by reducing the pressure ratio of cracking gas compressor IV section, increase the pressure ratio of V section, make the working pressure of high pressure depropanizer 1 lower than conventional pressure, the pressure of conventional high pressure depropanizer is generally more than 1.6MPa, and the pressure-controlling of high pressure depropanizer 1 of the present invention is at 1.3～1.5MPa; Low pressure depropanizing tower tower top arranges a return wire, C3 component is partly refluxed to high pressure depropanizer, the partition ratio that regulates C3 component in high pressure depropanizer tower reactor is that C3 component accounts for the 25-45% that enters the total C3 amount of high-pressure tower, make tower reactor temperature be controlled at 70-80 DEG C, reduce tower reactor temperature, effectively stop the polymerization of C4 component, reduce reboiler fouling and column plate and stop up; In addition, lighter hydrocarbons stripping tower also can be further set in technique, for the above heavy constituent of C3 of IV, the intersegmental separating tank of V bottom component is separated in advance, comprising most of C4 unsaturated hydrocarbons, these heavy constituents directly enter low pressure depropanizing tower, stride across high pressure depropanizer, because C4 unsaturated hydrocarbons content in high pressure depropanizer charging reduces, tower reactor temperature can decline, and can further reduce tower reactor fouling.Use technique of the present invention in the situation that not using stopper, the tower reactor temperature of high pressure depropanizer is controlled in 80 DEG C, prevent or reduce reboiler fouling, column plate obstruction, increase turndown ratio, make the steady long-time running of device.
Above-described embodiment is described the preferred embodiment of the present invention; not scope of the present invention is limited; design under the prerequisite of spirit not departing from the present invention; various distortion and improvement that those of ordinary skill in the art make technical scheme of the present invention, all should fall in the definite protection domain of the claims in the present invention book.
Claims (6)
1. one kind is reduced the Technical analysis technique of reboiler fouling, described double tower comprises high pressure depropanizer and low pressure depropanizing tower, compressor is provided with the compression of I-V section altogether, every intersegmental intersegmental separating tank that is provided with, unstripped gas is after the compression of I-IV section, enter high pressure depropanizer through alkali cleaning with after being dried, the C3 of high pressure depropanizer tower reactor and above component enter low pressure depropanizing tower, high pressure depropanizer tower top C3 and a following component part are returned to high pressure depropanizer, it is characterized in that: a low pressure depropanizing tower tower top material part is returned to high pressure depropanizer, the pressure of high pressure depropanizer is 1.3-1.5MPa, in tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 25-45% to C3 component, tower reactor temperature is controlled at 70-80 DEG C, also comprise IV, the intersegmental separating tank of V bottom component enters lighter hydrocarbons stripping tower and isolates C3 and following component and C3 and above component, C3 and above component enter low pressure depropanizing tower, isolate C3 component, C4 and above component.
2. technique according to claim 1, it is characterized in that: described unstripped gas separates through the separation of I section entrance separating tank, compressor I to the compression of IV section, intersegmental separating tank, tank deck gaseous fraction enters in dryer feed separating tank after soda-wash tower alkali cleaning, isolate light hydrocarbon gas component and heavy hydrocarbon liquid component, the heavy hydrocarbon liquid component obtaining at the bottom of tank enters described lighter hydrocarbons stripping tower and isolates C3 and following component and C3 and above component.
3. technique according to claim 1 and 2, is characterized in that: described C3 and following component are returned to III, the intersegmental separating tank of IV.
4. technique according to claim 1, is characterized in that: the pressure of described high pressure depropanizing is 1.3-1.4MPa, and in tower reactor, to account for the molecular fraction of the total C3 component that enters high pressure depropanizer be 30-45% to C3 component, and tower reactor temperature is 70-75 DEG C.
5. technique according to claim 1, is characterized in that: the inlet pressure of described compression V section is 1.3-1.5MPa, and the top hole pressure of compression V section is 2.6-3.0 with the ratio of inlet pressure.
6. technique according to claim 1, is characterized in that: the top hole pressure of described compression IV section is 1.6-1.8MPa, and the top hole pressure of compression IV section is 1.8-2.0 with the ratio of inlet pressure.
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| CN103896702B (en) * | 2012-12-27 | 2016-06-08 | 中国石油天然气股份有限公司 | Light hydrocarbon separation method and system from middle precut of fraction |
| CN110734355B (en) * | 2018-07-18 | 2022-11-15 | 中国石化工程建设有限公司 | Energy-saving stable type ethylene hydrogenation separation process and device |
| CN111393251A (en) * | 2020-04-23 | 2020-07-10 | 上海卓然工程技术股份有限公司 | Double-effect differential pressure thermal coupling depropanization process method in propane dehydrogenation propylene preparation device |
| CN113354505A (en) * | 2021-03-19 | 2021-09-07 | 北京欧谊德科技有限公司 | Separation device and separation method for preventing catalytic gas fractionation device from coking at bottom of depropanizer |
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| CN1274649C (en) * | 2004-04-22 | 2006-09-13 | 中国石油化工股份有限公司 | Catalytic distillation process for olefin production device |
| CN101172929B (en) * | 2006-10-31 | 2010-05-19 | 中国石油化工股份有限公司 | One-stage extraction method for butadiene by NMP method |
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| 乙烯装置双塔脱丙烷操作条件探讨及优化;苟红霞等;《设计技术》;20021231;第12卷(第1期);第12-14页 * |
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