CN105617952A - Discharging system of fluidized bed reactor and method thereof - Google Patents
Discharging system of fluidized bed reactor and method thereof Download PDFInfo
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Abstract
The invention discloses a discharging system of a fluidized bed reactor and a method thereof. The system comprises a settlement container and a transfer container, an injector is arranged between the settlement container and the fluidized bed reactor, a pipeline of an inlet at the bottom is connected with an outlet at the top of the fluidized bed reactor, a pipeline a separated from the pipeline is connected with the inlet of the injector; a pipeline d at the upper part of the settlement container is connected with the bottom of the injector; the outlet of the injector is connected with the lower part of the fluidized bed reactor; a discharge pipeline b at the upper part of the fluidized bed reactor is connected with the top of the settlement container; a balance pipeline e is arranged between the top of the settlement container and the top of a transfer container; a main inlet valve is arranged on the pipeline a, a main drain valve A is arranged on the discharge pipeline b, a transfer valve is arranged on the pipeline d, and a main balance valve is arranged on the pipeline e. The discharging system of the fluidized bed reactor can obviously increase the discharging efficiency of a pressure vessel of a fluidized bed during a condensation state technology. Liquid content of the discharged materials is reduced, the burden of a degassing cabin is reduced, and energy consumption is reduced.
Description
Technical field
The present invention relates to fluidized-bed reactor field, furtherly, relate to a kind of discharge system and the method for fluidized-bed reactor.
Background technology
Polyethylene is that a class is produced by kinds of processes method, has the series of products thermoplasticity general-purpose plastics of various structures and characteristic, is one of the principal item of synthetic resin, is widely used in the fields such as agricultural, chemical industry, light industry, weaving, machinery and national defence. The method of industrial production polyethylene mainly has slurry polymerization process, solution polymerization process and gaseous polymerization three kinds. Wherein, gas-phase polyethylene technological process is simple, and production capacity is big, production chains is strong, eliminates the treatment process such as the refining of solvent and recovery, greatly reduces equipment investment expense and production operation expense, and environmentally friendly, thus become the main flow in polyethylene process.
Along with the development of national economy, the demand of polyvinyl resin is continuously increased, and the polyethylene production improving existing apparatus becomes the focus that industrial development is attracted attention. But, the biggest obstacle of restriction gas-phase polyethylene output increased is removing of reaction heat. In traditional gas-phase polyethylene technique, it is that reactor removes heat mainly through the temperature rise of circulating current, thus the space-time yield of polyethylene is subject to the restriction of fluidizing gas velocity, it is impossible to increase substantially. At the beginning of the eighties in last century, patent US4543399 and US4588790 discloses " gas-phase fluidized-bed polyethylene condensation pattern operating procedure " (referred to as " condensation process " or " condensing mode operation "). Condensation process is by introducing the liquid of easily condensation, i.e. cooling medium (being generally high ' alpha ' olefin or the inertia saturated hydrocarbons of copolymerization), it is made to evaporate in a fluidized bed reactor to strengthen removing of polymerization reaction heat, so that the space-time yield of reactor significantly improves. The appearance of frozen state technique indicates that polyethylene production technology obtains new breakthrough progress.
In condensation process, for discharging solid material from fluidized bed pressure vessel, gas-phase fluidized-bed pressure vessel or gas fluidised bed polymerisation container, there are many systems and known method. But, use existing discharge system and method to may result in problems with. First, cause the extra consumption of the reactant of exhaust system, specifically, because pore volume in granule and about is filled with high pressure gas mixture, a large amount of gases lost or gas/liquid mixture. Then, the gas of loss must be supplemented with (consuming extra raw material) or by compressing, be re-circulated in system with pump condensation or these combination. In either case, waste raw material and consumed energy. Secondly, in condensation process, the fluidized-bed polymerization reactor condensed fluid content as described in patent 201110290787.6 is up to 10wt%, and condensed fluid generally passes into from fluidized-bed reactor bottom, and the condensed fluid content of bed bottom material is higher. If therefore adopting traditional discharging technology, due to material condensed fluid too high levels, in the process from the discharging pipeline discharging of the nearly distribution grid in fluid bed bottom, material easily blocks discharging pipeline and discharge velocity is slow. The more important thing is, more condensed fluid taken out of by the material of discharge, and this not only causes a large amount of losses of condensed fluid in reactor, and increases the operational load of degassing cabin.
Patent US200780037815.5 and US200780034097.6 discloses a kind of discharge system going out solid/gas mixture from fluidized bed pressure vessel. As mentioned, open the discharge valve between fluidized bed pressure vessel and sedimentation vessel, solid and gas-pressurized and enter sedimentation vessel. The top of sedimentation vessel connects pipeline to the second of area of low pressure, reactor top and provides the flow channel returning reactor for gas, and solid settles and is filled primarily with sedimentation vessel simultaneously. Then all being closed by two valves, keep sedimentation vessel to be full of solid particle, but have interstitial space between the granule of gassy mixture, sedimentation vessel is under reactor pressure completely. Describe the sedimentation vessel at the discharge system of patent US200780037815.5 and generally comprise hemisphere upper cover, straight section and tapered bottom end.
After sedimentation vessel separates from fluidized bed pressure vessel, then valve is opened and solid is transferred to transfer vessel. When solid flows into transfer vessel, pressure equilibrium also occurs between transfer vessel and sedimentation vessel. When completing, the pressure of transfer vessel and sedimentation vessel is also in moderate degree. But, transfer vessel still comprises substantial amounts of gas between granule. Then some implementers open cross link valve and make medium pressure gas be sent to the empty transfer vessel balanced each other in another group. As long as the pressure in transfer vessel is relatively low, product is transferred to other containers wherein only having the transfer of a small amount of gas-pressurized being used for additionally processing. The gas being retained in sedimentation vessel is transferred back to fluidized bed pressure vessel during the next one fills circulation.
As above described in patent, although decrease the reactant loss in the discharge system of fluidized bed pressure vessel and energy expenditure. But for the fluidized bed pressure vessel in condensation process, the discharging effect of above-mentioned discharge system is all undesirable, and energy expenditure is bigger, it is easier to produce fault, it is impossible to meet the discharging requirement of current novel process.
Accordingly, it would be desirable to a kind of novel discharging technology, it can improve the discharging efficiency of fluidized bed pressure vessel. In process of production, this technique is better to the product material discharge effect of fluidized bed pressure vessel in condensation process, consuming little energy, and it is relatively stable to control discharge velocity, is greatly reduced in discharging process Balance Air loss.
Summary of the invention
For solving produced problem in prior art, the invention provides the discharge system of a kind of fluidized-bed reactor and method. The present invention can significantly improve the discharging efficiency of fluidized bed pressure vessel in frozen state technique. By adding injection apparatus in original discharge system, Balance Air in injection apparatus suction sedimentation vessel is utilized to form it into negative pressure so that many warm areas fluidized-bed reactor realizes upper outlet, reduces the content liquid giving off material, reduce the burden of degassing cabin, reduce energy consumption.
An object of the present invention is to provide the discharge system of a kind of fluidized-bed reactor.
Including: sedimentation vessel and transfer vessel,
Being provided with ejector between sedimentation vessel and fluidized-bed reactor, fluidized-bed reactor top exit connects the pipeline of bottom inlet and separates a by-pass line a connection ejector import; Sedimentation vessel upper pipeline d connects bottom ejector; Ejector outlet connects fluidized-bed reactor bottom; Fluidized-bed reactor top discharge line b connects sedimentation vessel top; Connect transfer vessel bottom sedimentation vessel, balance pipeline e is set between sedimentation vessel top and transfer vessel top;
Pipeline a arranges master air suction valve, discharge line b arranges main drain valve A, pipeline d arranges transfer valve, pipeline e arranges main balanced valve.
Fluidized-bed reactor bottom can also connect sedimentation vessel top by discharge line c; Discharge line c arranges main drain valve B.
Line b and line c can be respectively arranged with cleaning gas purging entrance.
Preferred:
The setting height(from bottom) 2m more than higher than fluidized-bed reactor top discharge line of ejector;
The discharging pipeline horizontal section length of fluidized-bed reactor is not more than 1.5m.
The two of the purpose of the present invention are to provide the discharging method of a kind of fluidized-bed reactor.
Including:
Opening master air suction valve and transfer valve, regulating the circulating air flow entering ejector is 5t/h-15t/h, the gas in sprayer pumps sedimentation vessel, by sedimentation vessel Stress control 1.0-2.5Mpa, opening main drain valve A, under differential pressure action, product enters sedimentation vessel from top discharge line b.
When fluidized-bed reactor arranges bottom discharging pipeline,
Opening main drain valve A and main drain valve B, under differential pressure action, product enters sedimentation vessel from top discharge line b and bottom discharge line c.
After discharging terminates, close the transfer valve on outlet valve and pipeline d, open the main balanced valve on pipeline e, gas phase mixing in sedimentation vessel and transfer vessel reaches balance, two container gaseous pressures are equal, solid material in sedimentation vessel falls under gravity into transfer vessel, followed by relating in discharge system pressure equalization between different vessels, final realization is reduced pressure step by step, the gaseous monomer of solvent in solid material is made constantly to parse, before guaranteeing to send into degassing cabin, the concentration of gaseous monomer drops to certain value.
Top discharge line b and bottom discharge line c is purged by cleaning gas.
The present invention specifically can be by the following technical solutions:
Discharge system includes: comprise the sedimentation vessel of conical top cover; Ejector with sedimentation vessel fluid communication; Transfer vessel with sedimentation vessel fluid communication; The transfer valve of the gas flow shifted from sedimentation vessel to sprayer pumps is controlled between sedimentation vessel and ejector; Control circulating current master air suction valve from fluidized-bed reactor inlet line to ejector; Fluidly connect the fluidized bed pressure vessel discharge line to sedimentation vessel; Control the main exit valve of the fluid mixture rate of discharge from transfer vessel.
It is provided above ejector at sedimentation vessel, fluidized-bed reactor import circulating current controls after flow through tap line and by master air suction valve, enter ejector, the gas that ejector is aspirated in sedimentation vessel by the pipeline being connected with sedimentation vessel makes it be internally formed negative pressure, pressure 0.01��0.1Mpa in fluidized-bed reactor upper part discharge port place pressure is more than sedimentation vessel, the material in reactor flows into sedimentation vessel under the promotion of pressure reduction.
Fluidized-bed reactor can be provided with two discharging pipelines, is at nearly material level place, reactor top and the nearly distribution grid place of reactor lower part respectively, in fluidized-bed reactor discharging process, it is possible to open two outlet valves simultaneously. This discharging method enables to reactor faster discharge, and arranges two outlet valves and so that whole discharging process operation is flexible, implementer can be facilitated to select discharge method as the case may be.
Fluidized bed circulation gas pipeline is provided with tap line in order to provide ejector working media, tap line is provided with master air suction valve and regulates the flow of circulating air. This being designed to accurately controls and regulates the circulating air flow and ratio that enter ejector, keeps stablizing of flow on circulating air main line, can also control the negative pressure that ejector can be generated by simultaneously flexibly, control reactor discharge velocity.
Entering the circulating air flow of ejector at 5t/h-15t/h, thus ensureing that ejector can form sufficiently large negative pressure, the gas-solid mixture of fluidized-bed reactor can smoothly enter in sedimentation vessel.
The present invention can comprise the exhaust line fluidly connecting sedimentation vessel top and ejector and the control transfer valve by the extraction flow of exhaust line.
The Balance Air entered in sedimentation vessel with material in discharging process can enter to be incorporated to circulating air pipeline by sprayer pumps, and can pass through to regulate the circulating air flow entering ejector, control the vacuum magnitude formed, and then the Balance Air of sedimentation vessel is aspirated return fluidized-bed reactor.
The discharging pipeline horizontal section length of fluidized-bed reactor is not more than 1.5m, and material so can be made to flow into more easily in sedimentation vessel, it is prevented that material is built up at horizontal segment.
The setting height(from bottom) of ejector is more than 2m on upper outlet pipeline, higher than inside reactor resin material level, it is prevented that siphon.
When being embodied as, the system of the present invention can also include the device of detection abnormal conditions, as included automatic control system and the device of detection pressure, flow, temperature, enclosure stress, valve position or actuator position.
Circulating current enters the master air suction valve of ejector and opens, and circulating air passes through ejector periodic duty always, and when discharging, opens the air bleeding valve of the exhaust line connected with sedimentation vessel top.
The solids monitoring device that sedimentation vessel is full of can also be comprised detecting when, comprise the purging of the dry gas of input sedimentation vessel, and comprise the cleaning gas purging of input exhaust line.
Other specific embodiments of the method for the present invention can include the step of cleaning-gas purging discharge line, cleaning-gas purging exhaust line, dry gas purging sedimentation vessel or dry gas purging transfer vessel.
In other specific embodiments, the solid material of a discharging process discharge generally at least fills the volume of the 80% of sedimentation vessel.
It is an advantage of the current invention that discharge system and the method by adopting the present invention, it is possible to significantly improve the discharging efficiency of fluidized bed pressure vessel in frozen state technique. By adding injection apparatus in original discharge system, Balance Air in injection apparatus suction sedimentation vessel is utilized to form it into negative pressure so that many warm areas fluidized-bed reactor realizes upper outlet, reduces the content liquid giving off material, reduce the burden of degassing cabin, reduce energy consumption. Meanwhile can enter the flow of circulating current in injection apparatus by adjustment and regulate the pressure reduction between fluidized bed pressure vessel and sedimentation vessel, and then control discharge velocity, it is achieved stablize discharging. It is designed with outlet valve, it is possible to facilitate implementer to switch over according to concrete operations condition so that whole draw operation becomes easily-controllable flexibly in reactor top and the bottom. Balance Air in discharging Settlement container can ceaselessly be aspirated by ejector and be incorporated to circulating air pipeline, reduces loss and the energy loss of unstripped gas compared to tradition discharging technology.
Accompanying drawing explanation
Fig. 1 is the fluidized-bed reactor discharge system schematic diagram of the present invention;
Fig. 2 is emitter construction schematic diagram;
Fig. 3 is injector nozzle structural representation;
Description of reference numerals:
1 fluidized-bed reactor; 5 main balanced valves; 6 transfer vessels; 8 master air suction valves; 11 sedimentation vessel; 12 transfer valve; 14 main drain valve B; 17 main drain valve A; 18 ejectors; 22 gas distributors; 23 clean gas; 25 recycle gas compressors; 26 recycle gas cooler;
31 receiving chamber; 32 nozzles; 33 mixing chambers; 34 bubblers; 35 working fluids; 36 driving fluids
Detailed description of the invention
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment 1
As shown in Figure 1, a kind of discharge system of fluidized-bed reactor, including: sedimentation vessel 11 and transfer vessel 6, being provided with ejector 18 between sedimentation vessel 11 and fluidized-bed reactor 1, fluidized-bed reactor 1 top exit connects the pipeline of bottom inlet and separates by-pass line a connection ejector 18 import; Sedimentation vessel 11 upper pipeline d connects bottom ejector 18; Ejector 18 outlet connects fluidized-bed reactor 1 bottom; Fluidized-bed reactor 1 top discharge line b and bottom discharge line c connects sedimentation vessel 11 top; Connect transfer vessel 6 bottom sedimentation vessel 11, balance pipeline e is set between sedimentation vessel 11 top and transfer vessel 6 top;
Pipeline a arranges master air suction valve 8, discharge line b arranges main drain valve A17, discharge line c arranges main drain valve B14, pipeline d arranges transfer valve 12, pipeline e arranges main balanced valve 5.
Line b and line c can be respectively arranged with cleaning gas purging entrance.
The setting height(from bottom) of ejector is higher than fluidized-bed reactor top discharge line 2 meters;
The discharging pipeline horizontal section length of fluidized-bed reactor is 1.5 meters.
Fluidized-bed reactor upper outlet pipeline arranges ball valve two, two, elbow. The solid material of discharging process discharge generally at least fills the volume of the 80% of sedimentation vessel.
Discharge product linear low density polyethylene (LLDPE), wherein ejector 18 selects the ejector shown in Fig. 2, and the nozzle of ejector selects the nozzle shown in Fig. 3. Fluidized-bed reactor top bed temperature is about 88 DEG C, and pressure is about 2.35MPa, and fluidized-bed reactor 1 bottom passes into condensed fluid, and condensed fluid content is about 5wt%, and temperature is about 60 DEG C. When reactor material level reaches 15.9m, adopt upper outlet method, open transfer valve 12 and master air suction valve 8, regulating the circulating air flow entering ejector 18 is 9t/h, now ejector 18 aspirates the gas in sedimentation vessel 11, by sedimentation vessel Stress control at about 2.0MPa, opens main drain valve A17, under differential pressure action, product is discharged from top discharge line. In output streams, each composition flow rate is: LLDPE powder 40t/h, nitrogen 3065kg/h, hydrogen 254kg/h, ethylene 1346kg/h, hexene 182kg/h, methane 86kg/h, ethane 67kg/h. Wherein ethylene and hexene are unreacted monomers, do not have liquid in output streams. The fault rates such as compared to the discharging technology disclosed by patent US200780037815.5 and US200780034097.6, this discharging method causes, discharging pipeline blocking reduce by 91%. In subsequent product degasification process, degassing cabin nitrogen is purged temperature and is adjusted to 80 DEG C, now hydrocarbon content in material is reduced to the N needed for 20ppm2Amount reduction by 50%.
Embodiment 2
System is with embodiment 1.
Discharge product linear low density polyethylene (LLDPE), wherein ejector 18 selects the ejector shown in Fig. 2, and the nozzle of ejector selects the nozzle shown in Fig. 3. Under certain operating conditions, fluidized-bed reactor top bed temperature is about 86 DEG C, and pressure is about 2.35MPa, and fluidized-bed reactor 1 bottom passes into condensed fluid, and condensed fluid content is about 6wt%, and temperature is about 57 DEG C. When reactor material level reaches 15.9m, adopt upper outlet method, open transfer valve 12 and master air suction valve 8, regulating the circulating air flow entering ejector 18 is 9t/h, now ejector 18 aspirates the gas in sedimentation vessel 11, by sedimentation vessel Stress control at about 2.0MPa, opens main drain valve A17, under differential pressure action, product is discharged from top discharge line. In output streams, each composition flow rate is: LLDPE powder 40t/h, nitrogen 3000kg/h, hydrogen 240kg/h, ethylene 1300kg/h, hexene 200kg/h, methane 95kg/h, ethane 70kg/h. Wherein ethylene and hexene are unreacted monomers, do not have liquid in output streams. The fault rates such as compared to the discharging technology disclosed by patent US200780037815.5 and US200780034097.6, this discharging method causes, discharging pipeline blocking reduce by 90%. In subsequent product degasification process, degassing cabin nitrogen is purged temperature and is adjusted to 82 DEG C, now hydrocarbon content in material is reduced to the N needed for 20ppm2Amount reduction by 52%.
Embodiment 3 (top and the bottom discharging simultaneously)
System is with embodiment 1.
Discharge product linear low density polyethylene (LLDPE), wherein ejector 18 selects the ejector shown in Fig. 2, and the nozzle of ejector selects the nozzle shown in Fig. 3. Under certain operating conditions, fluidized-bed reactor top bed temperature is about 90 DEG C, and pressure is about 2.35MPa, and fluidized-bed reactor 1 bottom passes into condensed fluid, and condensed fluid content is about 4.5wt%, and temperature is about 65 DEG C. When reactor material level reaches 15.9m, adopt upper outlet method, open transfer valve 12 and master air suction valve 8, regulating the circulating air flow entering ejector 18 is 9t/h, now ejector 18 aspirates the gas in sedimentation vessel 11, by sedimentation vessel Stress control at about 2.0MPa, opens main drain valve A17 and main drain valve B14, under differential pressure action, product is discharged respectively from top discharge line and bottom discharging pipeline. In upper pipeline output streams, each composition flow rate is: LLDPE powder 35t/h, nitrogen 2600kg/h, hydrogen 225kg/h, ethylene 1180kg/h, hexene 100kg/h, methane 60kg/h, ethane 40kg/h. The each composition flow rate of bottom discharging pipeline output streams is: LLDPE powder 5t/h, nitrogen 400kg/h, hydrogen 35kg/h, ethylene 170kg/h, hexene 90kg/h, methane 25kg/h, ethane 20kg/h. Wherein ethylene and hexene are unreacted monomers, with a small amount of condensed fluid in the output streams of bottom discharging pipeline. The fault rates such as compared to the discharging technology disclosed by patent US200780037815.5 and US200780034097.6, this discharging method causes, discharging pipeline blocking reduce by 80%. In subsequent product degasification process, degassing cabin nitrogen is purged temperature and is adjusted to 78 DEG C, now hydrocarbon content in material is reduced to the N needed for 20ppm2Amount reduction by 35%.
Claims (7)
1. a discharge system for fluidized-bed reactor, including: sedimentation vessel and transfer vessel, it is characterised in that:
Being provided with ejector between sedimentation vessel and fluidized-bed reactor, fluidized-bed reactor top exit connects the pipeline of bottom inlet and separates a by-pass line a connection ejector import; Sedimentation vessel upper pipeline d connects bottom ejector; Ejector outlet connects fluidized-bed reactor bottom; Fluidized-bed reactor top discharge line b connects sedimentation vessel top; Connect transfer vessel bottom sedimentation vessel, balance pipeline e is set between sedimentation vessel top and transfer vessel top;
Pipeline a arranges master air suction valve, discharge line b arranges main drain valve A, pipeline d arranges transfer valve, pipeline e arranges main balanced valve.
2. the discharge system of fluidized-bed reactor as claimed in claim 1, it is characterised in that:
Fluidized-bed reactor bottom discharge line c connects sedimentation vessel top; Discharge line c arranges main drain valve B.
3. the discharge system of fluidized-bed reactor as claimed in claim 2, it is characterised in that:
Line b and line c are respectively arranged with cleaning gas purging entrance.
4. the discharge system of fluidized-bed reactor as claimed in claim 1, it is characterised in that:
The setting height(from bottom) 2m more than higher than fluidized-bed reactor top discharge line of ejector;
The discharging pipeline horizontal section length of fluidized-bed reactor is not more than 1.5m.
5. the discharging method adopting fluidized-bed reactor as claimed in claim 1, it is characterised in that described method includes:
Opening master air suction valve and transfer valve, regulating the circulating air flow entering ejector is 5t/h-15t/h, the gas in sprayer pumps sedimentation vessel, by sedimentation vessel Stress control at 1.0-2.5Mpa, opening main drain valve A, under differential pressure action, product enters sedimentation vessel from top discharge line b.
6. the discharging method of fluidized-bed reactor as claimed in claim 5, it is characterised in that:
Opening main drain valve A and main drain valve B, under differential pressure action, product enters sedimentation vessel from top discharge line b and bottom discharge line c.
7. the discharging method of fluidized-bed reactor as claimed in claim 6, it is characterised in that:
Top discharge line b and bottom discharge line c is purged by cleaning gas.
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| CN103657538A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Method for loading and unloading catalysts for fixed fluidized bed reactor |
| CN103908930A (en) * | 2014-03-31 | 2014-07-09 | 神华集团有限责任公司 | Method for cleaning distribution plate of fluidized bed reactor and control system of method |
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|---|---|---|---|---|
| US6056927A (en) * | 1996-08-23 | 2000-05-02 | Bp Chemicals Limited | Equipment and process for gas-phase olefin polymerization |
| US20010024625A1 (en) * | 2000-02-28 | 2001-09-27 | Olson Robert Darrell | Polyolefin production using condensing mode in fluidized beds, with liquid phase enrichment and bed injection |
| CN101448921A (en) * | 2006-03-08 | 2009-06-03 | 尤尼威蒂恩技术有限公司 | Polymerization process and apparatus |
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