CN202808647U - Crude methanol synthetic system - Google Patents
Crude methanol synthetic system Download PDFInfo
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- CN202808647U CN202808647U CN2012205055473U CN201220505547U CN202808647U CN 202808647 U CN202808647 U CN 202808647U CN 2012205055473 U CN2012205055473 U CN 2012205055473U CN 201220505547 U CN201220505547 U CN 201220505547U CN 202808647 U CN202808647 U CN 202808647U
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Abstract
本申请提供了一种粗甲醇合成系统。粗甲醇合成系统包括：浆态床反应器，在浆态床反应器中反应气在催化剂作用下产生生成气；旋风分离器，与浆态床反应器之间具有生成气输送管线和催化剂回流管线；惰性溶剂回收系统，设置在浆态床反应器与旋风分离器之间的生成气输送管线的延伸管线上，且与浆态床反应器之间具有惰性溶剂回流管线；粗甲醇回收系统，与惰性溶剂回收系统相连通并处理来自惰性溶剂回收系统的生成气得到分离的粗甲醇和循环气，且粗甲醇回收系统与浆态床反应器之间具有供至少部分循环气进入浆态床反应器的进气管线。本实用新型的粗甲醇合成系统避免了催化剂的浪费以及对装置的堵塞；在浆态床反应器中催化剂与反应气充分接触提高甲醇产率。
The application provides a crude methanol synthesis system. The crude methanol synthesis system includes: a slurry bed reactor, in which the reaction gas generates gas under the action of a catalyst; a cyclone separator, with a gas delivery line and a catalyst return line between the slurry bed reactor and the slurry bed reactor The inert solvent recovery system is arranged on the extension pipeline of the generated gas delivery pipeline between the slurry bed reactor and the cyclone separator, and has an inert solvent return line between the slurry bed reactor and the crude methanol recovery system, and The inert solvent recovery system is connected to and processes the generated gas from the inert solvent recovery system to obtain separated crude methanol and cycle gas, and there is a device between the crude methanol recovery system and the slurry bed reactor for at least part of the cycle gas to enter the slurry bed reactor intake pipeline. The crude methanol synthesis system of the utility model avoids the waste of the catalyst and the blockage of the device; in the slurry bed reactor, the catalyst is fully contacted with the reaction gas to improve the methanol yield.
Description
Technical field
The utility model relates to the synthetic field of methyl alcohol, in particular to a kind of thick system for methanol synthesis.
Background technology
In methanol production process, usually because the reaction bed temperature in the synthesis reactor is uneven or temperature of reaction is too high or cross reaction temperature spend low or reaction gas in methanol content too high, cause by product too much, such as methane and wax etc.Wax can reduce the heat transfer effect of methanol-water cooler, the separating effect of reduction methanol separator on the one hand, carries methyl alcohol in the circulation gas secretly thereby make, and then has reduced the per pass conversion of synthetic tower; Wax is bonded on pipeline and the column plate on the other hand, can reduce circulation area, even result in blockage; And behind downstream unit, in case temperature reduces, the wax in the thick methyl alcohol will condense, and has influence on the normal production of downstream unit.
For, ammonia synthesis and CO conversion this class gas-solid synthetic by the lower methylamine of pressurization, methyl ether, methyl alcohol exothermic catalytic reaction mutually, along with the carrying out of reaction, the reaction heat of constantly emitting improves reaction bed temperature.In order to reduce the efficient of by product and raising reactor, need to shift out reaction heat so that temperature of reaction is in a rational scope.
In industrial reactor, once widely a kind of of use was the multistage insulation reactor, reduce the reaction gas temperature with the unstripped gas Quench between two sections, this reactor has also reduced reactant concn during because of the unstripped gas Quench when reducing the reaction gas temperature, affected combined coefficient.Another kind is the shell and tube reactor for the synthetic Lurgi company of methyl alcohol, lower tubesheet and many pipes between tube sheet in housing, having, catalyzer is housed in the pipe, unstripped gas enters from the top inlet mouth and is distributed to each pipe, synthesizing methanol in the catalyst layer of installing in pipe, lateral inflow between pipe, the water boiling is continuously removed heat between pipe thereby the heat in the pipe makes, the steam that the water boiling produces is gone out by the side pipe, and reaction gas goes out tower by the bottom escape pipe.This tower has a narrow range of temperature, but the catalyst filling coefficient is little, and reaction efficiency is low.
At present, widely used is the methyl alcohol synthetic technology of DAVY company exploitation.As shown in Figure 1, catalyst loading produces middle pressure steam at the shell-side of reactor in the pipe; Fresh reaction gas enters from the pipe core 301 ' of reactor bottom; Gas is the beds by reactor from inside to outside radially; Then upwards flow in the bottom that the feedwater that comes from drum enters reactor by heat transfer tube 302 ' and the reaction heat that the methyl alcohol building-up reactions produces is taken away in the part vaporization; Temperature of reaction is regulated by the pressure of steam in the control tube.
At present, DAVY technology synthesizing methanol flow process as shown in Figure 2, synthetic virgin gas enters synthesic gas compressor 1 ' and compresses, and mixes the formation gas mixture through most of virgin gas after the synthesic gas compressor 1 ' supercharging with the circulation gas that the second methanol separator 5 ' comes; Then gas mixture enters the first synthetic tower 3 ' after the preheating first in the first synthesis loop intermediate heat 2 ', in the first synthetic tower 3 ', the methyl alcohol building-up reactions is carried out under highly active copper-based catalysts effect, and this reaction is thermopositive reaction, reaction heat by-product low-pressure steam; Reaction generates carries out preheating to wanting into the gas mixture of tower through the first synthesis loop intermediate heat 2 ' after gas leaves the first synthetic tower 3 ', then enters water cooler 4 ' and cools off; Circulation gas in the reaction generation gas enters the first methanol separator 5 ' with thick methyl alcohol to be separated.Isolated circulation gas and enter in addition recycle gas compressor 6 ' after the fresh synthesis gas mixing of part after synthetic air compressor 1 ' supercharging and enter again preheating in the second inlet tower gas preheater 7 ' after compressed in the first methanol separator 5 ', then enter the second synthetic tower 8 ', the second synthetic tower 8 ' same by-product low-pressure steam, after the reaction of leaving the second synthetic tower 8 ' generates gas 7 ' preheating enters the inlet tower gas of the second synthetic tower 8 ' in advance through the second synthesis loop intermediate heat, enter the second water cooler 9 ', reaction generates in the gas in the second water cooler 9 ' circulation gas and thick methyl alcohol enter the second methanol separator 10 ', and isolated thick methyl alcohol removes methyl alcohol flash drum 11 ' through behind the filter in the first methanol separator 5 ' and the second methanol separator 10 '.In the second methanol separator 10 ' major part of isolated circulation gas with enter synthesic gas compressor 1 ' after synthetic virgin gas is mixed.Simultaneously, need emit a part of off-gas to keep the rare gas elementes such as methane in the circulation gas and nitrogen within certain concentration range.
But also there are this some deficiencies in this technology itself, such as in the methanol sythesis reactor because reaction gas skewness in methanol sythesis reactor, cause that its and catalyzer are inhomogeneous to be contacted and then cause that methanol yield is low, catalyzer is wasted serious problem.
The utility model content
The utility model aims to provide a kind of thick system for methanol synthesis, to solve the problem that methanol yield is low in the prior art, the catalyzer waste is serious.
To achieve these goals, according to an aspect of the present utility model, provide a kind of thick system for methanol synthesis, thick system for methanol synthesis comprises: paste state bed reactor, and reaction gas produces under catalyst action and generates gas in paste state bed reactor; Cyclonic separator, and have the letter shoot line of generation and catalyzer reflux pipeline between the paste state bed reactor; The inert solvent recovery system is arranged on the extension pipeline of the generation letter shoot line between paste state bed reactor and the cyclonic separator, and and paste state bed reactor between have the inert solvent reflux pipeline; Thick methanol recovery system, be connected with the inert solvent recovery system and process from the generation of inert solvent recovery system and be so incensed that the thick methyl alcohol and the circulation gas that separate, and have the admission line that enters paste state bed reactor at least part of circulation gas between thick methanol recovery system and the paste state bed reactor.
Further, above-mentioned thick system for methanol synthesis also comprises: hydrogen recovery system, the hydrogen in the circulation gas that reclaims thick methanol recovery system that is connected with thick methanol recovery system; The reactive gas cleaning system, the end formation admission line that is connected with fresh reactant source of the gas and hydrogen recovery system has the pipeline that enters paste state bed reactor for the fresh reactant gas after purifying and hydrogen between the other end and the paste state bed reactor.
Further, above-mentioned paste state bed reactor comprises: bathing pool, be arranged on the top of paste state bed reactor, and have the outlet of the gas of generation on the housing at bathing pool top and be connected with cyclonic separator by generating the gas outlet; Have the catalyzer refluxing opening that is connected with cyclonic separator and the inert solvent refluxing opening that is connected with the inert solvent recovery system on the sidewall at bathing pool middle part; The bathing pool bottom has the middle vertex of a cone towards the conical bottom wall of below; Bathing pool inside is provided with gas distributor; The gas buffer chamber is arranged on the below of bathing pool.
Further, the gas distributor in the above-mentioned bathing pool comprises: central airway comprises: the air inlet supervisor, and an end is communicated with pipe connecting; Be used for spraying a plurality of eddy flow jet pipes of circumferential gyration airflow, one end communicates and circumferentially evenly arranging along the air inlet supervisor with air inlet supervisor's perisporium, the other end is pneumatic outlet, and the pneumatic outlet of each eddy flow jet pipe extends along the oblique below of the central axis that departs from the air inlet supervisor; The gas distribution tube group, centered by central airway, be arranged on central airway around, have the ventilating pit that communicates with the external world; Pipe connecting connects central airway and gas distribution tube group; The gas distribution tube group of gas distributor is fixed on the sidewall of bathing pool, and the air inlet of gas distributor supervisor extends to the diapire of bathing pool.
Further, above-mentioned gas distribution pipe group comprises at least two annular gas distribution pipes that arrange with one heart, pipe connecting is along the radially setting of gas distribution tube group and be communicated with each annular gas distribution pipe, ventilating pit is distributed on the tube wall of each annular gas distribution pipe, and the aperture arranges towards the below, ventilating pit comprises: the hole of cutting sth. askew, the sidewall in the hole of cutting sth. askew along the gas distribution tube group radially from inside to outside all to counterclockwise or all tilting to extend to clockwise direction; The first straight hole, the sidewall of the first straight hole vertically extends, and the first straight hole is intervally arranged at each annular gas distribution pipe with the hole of cutting sth. askew.
Further, the above-mentioned gas sparger also comprises the side airway that even number is communicated with pipe connecting, and the side airway is arranged on two pipe connectings between the annular gas distribution pipe in twos symmetrically with respect to central airway, and with the equidirectional extension of central airway.
Further, above-mentioned pipe connecting comprises: the first pipe connecting, and along the internal diameter extension of outermost annular gas distribution pipe, the center of passing gas distribution tube is communicated with each annular gas distribution pipe, and central airway is communicated with the center of the first pipe connecting; The second pipe connecting, vertical with the first pipe connecting, and be arranged between outermost annular gas distribution pipe and the most inboard annular gas distributed pipeline, each annular gas distribution pipe is communicated with, the side airway is communicated with the second pipe connecting.
Further, above-mentioned inert solvent recovery system comprises: the inert solvent condenser is arranged on the extension pipeline of the generation letter shoot line between paste state bed reactor and the cyclonic separator, and is connected with the pneumatic outlet of cyclonic separator; Drum, and have circulation line between the inert solvent condenser.
Further, above-mentioned thick methanol recovery system comprises the synthesis loop intermediate heat, air cooler, methanol separator, recycle gas compressor, condenser, circulating gas preheater, heat-eliminating medium feeding mechanism and thick methanol recovery device, methanol separator has liquid isolate outlet and the outlet of gaseous state isolate, condenser has thick methyl alcohol outlet and circulation gas outlet, the inert solvent condenser, the synthesis loop intermediate heat, air cooler is connected successively with methanol separator, and the liquid isolate outlet of methanol separator is communicated with thick methyl alcohol the first recovery line of formation with thick methanol recovery device; The gaseous state isolate outlet of methanol separator is connected with recycle gas compressor, the pneumatic outlet of recycle gas compressor is connected with condenser, the thick methyl alcohol outlet of condenser is communicated with thick methanol recovery device, and the circulation gas outlet of condenser is connected with paste state bed reactor and the synthesis loop intermediate heat is arranged in the circulation gas outlet and the pipeline between the paste state bed reactor of condenser; Hydrogen recovery system is connected with pipeline between methanol separator and the recycle gas compressor; The heat-eliminating medium feeding mechanism is connected with methanol separator and condenser respectively.
Further, above-mentioned thick methanol recovery system also comprises circulating gas preheater, be arranged in the circulation gas outlet and the pipeline between the synthesis loop intermediate heat of condenser, and circulating gas preheater is connected with drum.
Further, above-mentioned methanol separator comprises: the lime set withdrawing can, and liquid isolate outlet is arranged on the Lower Half of lime set withdrawing can; The scum dredger tank, the outlet of gaseous state isolate is arranged on the top of scum dredger tank; Upright radiator is connected with air cooler and heat-eliminating medium feeding mechanism respectively, and is arranged side by side above the lime set withdrawing can with the scum dredger tank, and the lime set withdrawing can is connected with upright radiator and scum dredger tank respectively.
Further, above-mentioned upright radiator is shell and tube cooler, and the tubulation two ends of upright radiator are connected with air cooler and lime set withdrawing can respectively, and the shell side of upright radiator is connected with the heat-eliminating medium feeding mechanism.
Further, the bottom of above-mentioned lime set withdrawing can is provided with wax discharging port, and is connected with catalytic cracking system by wax discharging port; The filling shell periphery that is positioned at liquid isolate outlet below of lime set withdrawing can is provided with well heater.
Further, above-mentioned condenser comprises: shell-and tube condenser, the pneumatic outlet of recycle gas compressor is connected with the tubulation of shell-and tube condenser, heat-eliminating medium feeding mechanism phase is connected with the shell side of condenser, liquid collecting tank is arranged on the bottom of shell-and tube condenser, is connected with the tubulation of shell-and tube condenser, thick methyl alcohol outlet is arranged on the bottom of liquid collecting tank, and the circulation gas outlet is arranged on the top of liquid collecting tank.
Further, above-mentioned heat-eliminating medium feeding mechanism comprises: the recirculated water feeding mechanism is connected with the shell side of upright radiator and shell-and tube condenser; The tempering air feeding mechanism comprises room air line of pipes and ambient air line of pipes, and room air line of pipes and ambient air line of pipes are connected with the shell side of upright radiator and shell-and tube condenser respectively.
Further, above-mentioned reactive gas cleaning system comprises: the fresh synthesis gas compressor is connected with hydrogen recovery system and fresh reactant source of the gas by gas feed; The reactive gas cleaning groove, an end is connected with the pneumatic outlet of fresh synthesis gas compressor, and the other end is connected with paste state bed reactor.
Thick system for methanol synthesis of the present utility model adopts paste state bed reactor as the device of catalyst reaction gas reaction, and reaction gas and catalyzer contact area under the effect of inert solvent increases, and then increases reaction efficiency, improves methanol yield; And the synthetic cost of thick methyl alcohol is saved in part heat but also recycle that inert solvent not only can be taken away in the paste state bed reactor in paste state bed reactor, cyclonic separator and the circulation of inert solvent recovery system simultaneously; The cyclonic separator that after paste state bed reactor, arranges not only can with catalyzer with generate that gas separate but also can be with the catalyst transport overfall state bed reactor after the cooling of separating, in this process, reclaimed catalyzer and avoided catalyzer with generating that gas enters that follow up device causes the catalyzer waste and to the obstruction of device.
Description of drawings
The Figure of description that consists of the application's a part is used to provide further understanding of the present utility model, and illustrative examples of the present utility model and explanation thereof are used for explaining the utility model, do not consist of improper restriction of the present utility model.In the accompanying drawings:
Fig. 1 shows the structural representation of the methanol sythesis reactor of DAVY company in the prior art;
Fig. 2 shows the structural representation of the system for methanol synthesis of DAVY company in the prior art;
Fig. 3 shows the synoptic diagram according to the thick system for methanol synthesis of a kind of embodiment of the utility model;
Fig. 4 shows the sectional view according to the gas distributor of a kind of preferred embodiment of the utility model, there is shown paste state bed reactor;
Fig. 5 shows the Q of gas distributor shown in Figure 4
1-Q
1To view;
Fig. 6 shows the Q of gas distributor shown in Figure 4
2-Q
2To view;
Fig. 7 shows the Q of gas distributor shown in Figure 4
4-Q
4To view;
Fig. 8 shows the sectional structure synoptic diagram according to the methanol separator of a kind of preferred embodiment of the utility model;
Fig. 9 shows the plan structure synoptic diagram of methanol separator shown in Figure 8; And
Figure 10 shows the sectional structure synoptic diagram according to the condenser of a kind of preferred embodiment of the utility model.
Embodiment
Need to prove that in the situation of not conflicting, embodiment and the feature among the embodiment among the application can make up mutually.Describe below with reference to the accompanying drawings and in conjunction with the embodiments the utility model in detail.
As shown in Figure 3, in a kind of typical embodiment of the utility model, a kind of thick system for methanol synthesis is provided, this thick system for methanol synthesis comprises paste state bed reactor 1, cyclonic separator 10, inert solvent recovery system and thick methanol recovery system, and paste state bed reactor 1 reaction gas in paste state bed reactor 1 produces under catalyst action and generates gas; Have the letter shoot line of generation and catalyzer reflux pipeline between cyclonic separator 10 and the paste state bed reactor 1; The inert solvent recovery system is arranged on the extension pipeline of the generation letter shoot line between paste state bed reactor 1 and the cyclonic separator 10, and and paste state bed reactor 1 between have the inert solvent reflux pipeline; Thick methanol recovery system is connected with the inert solvent recovery system and processes from the generation of inert solvent recovery system and be so incensed that the thick methyl alcohol and the circulation gas that separate, and has the pipeline that confession part circulation gas enters paste state bed reactor 1 between thick methanol recovery system and the paste state bed reactor 1.
Thick system for methanol synthesis as shown in Figure 3, in paste state bed reactor 1, fresh reactant gas, hydrogen and circulation gas react under the effect of catalyzer and generate to generate gas, generate gas and enter the granules of catalyst of wherein carrying secretly behind the cyclonic separator 10 and be separated then to return and proceed reaction in the paste state bed reactor 1; Remaining gaseous substance continues to be transported to the inert solvent recovery system through generating the letter shoot line, and inert solvent further separates with the generation gas of gaseous state and returns in the paste state bed reactor 1 in the inert solvent recovery system; Generate gas and after the inert solvent recovery system, enter thick methanol recovery system, treated thick methyl alcohol and the circulation gas that obtains separating in thick methanol recovery system, and carry out processing or collection or the utilization of bottom.
Above-mentioned thick system for methanol synthesis adopts paste state bed reactor 1 as the device of catalyst reaction gas reaction, and reaction gas and catalyzer contact area under the effect of inert solvent increases, and then reaction efficiency increases; And the synthetic cost of thick methyl alcohol is saved in part heat but also recycle that inert solvent not only can be taken away in the paste state bed reactor 1 in paste state bed reactor 1, cyclonic separator 10 and the circulation of inert solvent recovery system simultaneously; The cyclonic separator 10 that after paste state bed reactor 1, arranges not only can with catalyzer with generate that gas separate but also can be with the catalyst transport overfall state bed reactor 1 after the cooling of separating, in this process, reclaimed catalyzer and avoided catalyzer with generating that gas enters that follow up device causes the catalyzer waste and to the obstruction of device.
As shown in Figure 3, above-mentioned thick system for methanol synthesis also comprises hydrogen recovery system and reactive gas cleaning system, the hydrogen recovery system hydrogen in the circulation gas that reclaims thick methanol recovery system that is connected with thick methanol recovery system; The reactive gas cleaning system one end formation admission line that is connected with fresh reactant source of the gas and hydrogen recovery system has the pipeline that enters paste state bed reactor 1 for the fresh reactant gas after purifying and hydrogen between the other end and the paste state bed reactor 1.
In thick Production of methanol, for fear of poisoning of catalyst, the reaction gas that enters paste state bed reactor 1 is carried out purifying treatment remove the impurity that makes poisoning of catalyst; And, reaction gas (CO+H
2) in paste state bed reactor 1, be not to transform fully, unreacted CO, H
2And a small amount of rare gas element (N
2, Ar, CH
4) enter and become circulation gas after thick methanol recovery system is processed with generating gas, this circulation gas will with fresh reactant gas and hydrogen recovery system in hydrogen again enter paste state bed reactor 1 after gathering and react.In a kind of preferred embodiment, in order to reduce the inert component in the reaction gas, tell one gas as speeding to exit outer discharge system for methanol synthesis from circulation gas, for the utilization ratio that increases reaction gas and save cost, hydrogen recovery system is sent in the venting of speeding of this thigh, adopted hydrogen recovery system to reclaim the hydrogen in exitting of speeding of thick methanol recovery system.
As shown in Figure 4, paste state bed reactor 1 comprises bathing pool 100 and gas surge chamber 200 in a kind of preferred embodiment of the utility model, bathing pool 100 is arranged on the top of paste state bed reactor 1, has on the housing at bathing pool 100 tops to generate the gas outlet and be connected with cyclonic separator 10 by generating the gas outlet; Have the catalyzer refluxing opening that is connected with cyclonic separator 10 and the inert solvent refluxing opening that is connected with the inert solvent recovery system on the sidewall 102 at bathing pool 100 middle parts; Bathing pool 100 bottoms have the middle vertex of a cone towards the conical bottom wall of below; Bathing pool 100 inside are provided with gas distributor; Gas buffer chamber 200 is arranged on the below of bathing pool 100.
At paste state bed reactor 1 interior bathing pool 100 and the gas surge chamber 200 of arranging as shown in Figure 4, reaction gas and generation gas are separated, be conducive to improve the reaction efficiency of reaction gas under the effect of catalyzer; And be conducive to the even distribution of reaction gas in bathing pool at the bathing pool 100 interior gas distributors that arrange, and further increased the contact area of reaction gas and catalyzer, be conducive to increase methanol yield.
Such as Fig. 4, Fig. 5 and shown in Figure 7, gas distributor in the bathing pool 100 comprises central airway 280, gas distribution tube group 620 and pipe connecting 630, central airway 280 comprises air inlet supervisor 281 and is used for spraying a plurality of eddy flow jet pipes 282 of circumferential gyration airflow that an end of air inlet supervisor 281 is communicated with pipe connecting 630; One end of eddy flow jet pipe 282 communicates and circumferentially evenly arranging along air inlet supervisor 281 with air inlet supervisor 281 perisporium, the other end is pneumatic outlet, and the pneumatic outlet of each eddy flow jet pipe 282 extends along the oblique below of the central axis that departs from air inlet supervisor 281, gas distribution tube group 620 centered by central airway 280, be arranged on central airway 280 around, have the ventilating pit 650 that communicates with the external world; Pipe connecting 630 connects central airway 280 and gas distribution tube group 620; The gas distribution tube group 620 of gas distributor is fixed on the sidewall 102 of bathing pool 100, and the air inlet of gas distributor supervisor 281 extends to the diapire 103 of bathing pool 100.
Paste state bed reactor 1 with said structure, reaction gas is entered in the gas distribution tube group 620 of this gas distributor by central airway 280, and spread by ventilating pit 650, thereby realized gas equally distributed effect in being provided with the space of gas distributor downwards; When reaction gas diffused to the diapire of bathing pool 100 downwards, reaction gas was decelerated to zero and oppositely rises, and this round mobile and interaction in flow process of reaction gas makes reaction gas obtain Uniform Dispersion at equipment; And, the eddy flow jet pipes 282 that arrange the air inlet of central airway 280 supervisor 281 make reaction gas be responsible for 281 o'clock parts through air inlet by this eddy flow jet pipe 282 ejections, utilize the air pressure of reaction gas ejection that air-flow is risen, further optimized the effect of gas distribution.The distribution effect of reaction gas in paste state bed reactor 1 is better, more is conducive to catalyzer to the katalysis of reaction gas, more is conducive to improve the productive rate of methyl alcohol.Eddy flow jet pipe 282 can be arranged on same cross section of the air inlet supervisor 281 and circumferentially arrange, and also can be circumferentially arranged on air inlet supervisor 281 with spirrillum.
As shown in Figure 5 and Figure 6, the gas distribution tube group 620 of above-mentioned gas sparger comprises at least two annular gas distribution pipes 622 that arrange with one heart, 623,624, pipe connecting 630 is along the radially setting of gas distribution tube group 620 and be communicated with each annular gas distribution pipe 622,623,624, ventilating pit 650 is distributed in each annular gas distribution pipe 622,623, on 624 the tube wall, and the aperture arranges towards the below, ventilating pit 650 is included in the hole 652 and be projected as the first circular straight hole 651 on horizontal plane of cutting sth. askew that is projected as parallelogram on the horizontal plane, the sidewall in the hole 652 of cutting sth. askew along gas distribution tube group 620 radially from inside to outside all to counterclockwise or all tilting to extend to clockwise direction; The sidewall of the first straight hole 651 vertically extends, and the first straight hole 651 is intervally arranged on each annular gas distribution pipe 622,623,624 with the hole 652 of cutting sth. askew.
The gas that is entered by central airway 280 is distributed to each annular gas distribution pipe 622 by pipe connecting 630,623, in 624, and then by each annular gas distribution pipe 622, ventilating pit 650 on 623,624 is distributed to annular gas distribution pipe 622,623, around 624, realize gas distribution each position on every side to gas distributor; When gas when cutting sth. askew hole 652, gas can spread and backflow to gas distribution tube group 620 unlapped zones, thereby has improved the distribution of gas at each position of whole equipment; The first straight hole 651 is intervally arranged on annular gas distribution pipe 622,623,624 with the hole 652 of cutting sth. askew, can be with annular gas distribution pipe 622,623,624 upper gas dispersion have further been improved the distribution of gas to the zone of failing to cover between its zone that can cover and pipe.
As shown in Figure 5 and Figure 6, the above-mentioned gas sparger also comprises the side airway 380 that even number is communicated with pipe connecting 630, side airway 380 is arranged on two annular gas distribution pipes 622 in twos symmetrically with respect to central airway 280,623, on the pipe connecting 630 between 624, and with central airway 280 equidirectional extensions.Adopt central airway 280 and side airway 380 simultaneously to the gas distributor air inlet, reaction gas is entered in the gas distribution tube group 620 in more uniform mode, thereby thereby making each annular gas distribution pipe accept uniform intake method provide uniform gas distribution mode.
As shown in Figure 5 and Figure 6, above-mentioned gas sparger pipe connecting 630 comprises the first pipe connecting 631 and the second pipe connecting 632, the first pipe connecting 631 extends along the internal diameter of outermost annular gas distribution pipe 623, pass gas distribution tube 622,623,624 center is with each annular gas distribution pipe 622,623,624 are communicated with, and central airway 280 is communicated with the center of the first pipe connecting 631; The second pipe connecting 632 is vertical with the first pipe connecting 631, and be arranged between outermost annular gas distributed pipeline 623 and the most inboard annular gas distributed pipeline 622, with each annular gas distribution pipe 622,623,624 are communicated with, and side airway 380 is communicated with the second pipe connecting 632.
Orthogonal the first pipe connecting 631 and the second pipe connecting 632 are set in gas distributor, so that the gas in the gas distribution tube group 620 is at each annular gas distribution pipe 622,623, flowing between 624 is more smooth and easy; And, at the first pipe connecting 631 central airway 280 that is communicated with it is set, at the second pipe connecting 632 connected side airway 380 is set, the 620 while air feed from different guide pipelines to the gas distribution tube group, so that gas is distributed in each position of whole gas distribution tube group 620 sufficiently uniformly, for further providing good gas distribution basis from ventilating pit 650 diffusions.
As shown in Figure 3, above-mentioned thick system for methanol synthesis inert solvent recovery system comprises inert solvent condenser 2 and drum 3, inert solvent condenser 2 is arranged on the extension pipeline of the generation letter shoot line between paste state bed reactor 1 and the cyclonic separator 10, and is connected with the pneumatic outlet of cyclonic separator 10; Has circulation line between drum 3 and the inert solvent condenser 2; Being connected with inert solvent on this circulation line makes up line; When paste state bed reactor 1 liquid level descend to show that inert solvent reduces, make up line from inert solvent and to replenish new inert solvent and enter paste state bed reactor 1.
Adopt the inert solvent recovery system to be cooled to 100 ~ 140 ℃ through the generation gas that inert solvent condenser 2 was processed, the inert solvent cooling of carrying secretly in the reaction gas is condensed and return paste state bed reactor 1, realize the recycling of inert solvent, saved the synthetic cost of thick methyl alcohol; In with the process of reaction gas cooling, adopt and carry out heat exchange from the oiler feed in the drum 3 and reaction gas, become steam from the heat absorption of the oiler feed in the drum 3 and return drum 3, byproduct steam enters steam pipe system again so that this part heat energy is further recycled, and simultaneously oiler feed fills in the drum 3 with the material of maintenance drum and the balance of temperature.The oiler feed heat absorption becomes byproduct steam the part heat that the reaction that obtains in the paste state bed reactor 1 generates gas and inert solvent is taken out of, can absorption portion reaction heat after the condensed inert solvent of cooling returns paste state bed reactor 1, thereby the temperature of reaction in the reactor is maintained normal scope, avoid temperature of reaction to rise violently.Temperature of reaction in paste state bed reactor 1 can be stabilized in certain scope by above-mentioned circulation heat absorption, thereby has further improved reaction efficiency, improves methanol yield.
As shown in Figure 3, above-mentioned thick methanol recovery system comprises synthesis loop intermediate heat 12, air cooler 4, methanol separator 5, recycle gas compressor 6, condenser 7, circulating gas preheater 11, heat-eliminating medium feeding mechanism and thick methanol recovery device, methanol separator 5 has liquid isolate outlet and the outlet of gaseous state isolate, condenser 7 has thick methyl alcohol outlet and circulation gas outlet, inert solvent condenser 2, synthesis loop intermediate heat 12, air cooler 4 is connected successively with methanol separator 5, and the liquid isolate outlet of methanol separator 5 is communicated with thick methyl alcohol the first recovery line of formation with thick methanol recovery device; Methanol separator 5 is connected with recycle gas compressor 6 by the outlet of gaseous state isolate, the pneumatic outlet of recycle gas compressor 6 is connected with condenser 7, the thick methyl alcohol outlet of condenser 7 is communicated with thick methanol recovery device, the circulation gas of condenser 7 export be connected with paste state bed reactor 1 and circulation gas that circulating gas preheater 11 and synthesis loop intermediate heat 12 are successively set on condenser 7 exports and paste state bed reactor 1 between pipeline on; The gaseous state isolate outlet of methanol separator 5 is connected with hydrogen recovery system; The heat-eliminating medium feeding mechanism is connected with methanol separator 5 and condenser 7 respectively.
Generate gas after the inert solvent recovery system reclaims inert solvent, at first entering synthesis loop intermediate heat 12 and the reaction gas that is about to enter paste state bed reactor 1 carries out entering air cooler 4 after heat exchange cooling, the cooling and is cooled to 50 ~ 80 ℃, then 50 ~ 80 ℃ generation gas enters methanol separator 5 and further is cooled to about 45 ℃, wherein part methyl alcohol and wax are condensed, the methyl alcohol that condensation goes out enters thick methanol recovery device and reclaims, and wax regularly effluxes; The methyl alcohol that is not condensed and gas enter successively recycle gas compressor 6 and are pressurized to about 7～10MPa and temperature enters in the condenser 7 after rising to 60 ~ 95 ℃ and further cools off, temperature is down to about 35 ~ 75 ℃, the thick methyl alcohol that condensation is got off is transported to thick methanol recovery device, and remaining returns paste state bed reactor 1 as circulation gas and reacts; The methyl alcohol that is not condensed and gas portion gas before entering recycle gas compressor 6 enters the recovery that hydrogen recovery system carries out hydrogen; The heat-eliminating medium of methanol separator 5 and condenser 7 derives from the heat-eliminating medium feeding mechanism.
Carry out the rate of recovery that twice condensation further improved thick methyl alcohol to generating gas, and in methanol separator 5 with avoided under the wax condensation wax to downstream unit in because condensation and blocking pipeline, simultaneously, adopt condenser 7 that not isolated methyl alcohol in the methanol separator 5 is removed, reduced the methanol content in the circulation gas that returns paste state bed reactor 1, the generation that is conducive to reduce wax in Production of methanol also is conducive to keep the stable of methanol output.
As shown in Figure 3, thick methanol recovery system also comprises circulating gas preheater 11, be arranged in the circulation gas outlet and the pipeline between the synthesis loop intermediate heat 12 of condenser 7, and circulating gas preheater 11 is connected with drum 3.After carrying out first heat exchange absorbing heat through circulating gas preheater 11 after circulation gas is flowed out by the outlet of the circulation gas of condenser 7, continue to flow along pipeline, when flowing to synthesis loop intermediate heat 12, carry out further absorbing heat of the heat exchange second time, then continue to flow to paste state bed reactor 1 along pipeline.In the flow process of circulation gas, the circulating gas preheater 11 that arranges in the outlet of the circulation gas of condenser 7 adopts from the byproduct steam of drum to from condenser 7 circulation gas preheating out, what carry out heat exchange with circulation gas in circulating gas preheater 11 is from the byproduct steam in the drum 3, steam condensate is recyclable after the heat exchange, the generation gas that utilization is come by the inert solvent recovery system carries out again heat exchange with circulation gas in synthesis loop intermediate heat 12, the heat of system is reasonably utilized, and avoided causing when the circulation gas of low temperature returns paste state bed reactor 1 excessively reaction temperature to spend the low generation that causes too much wax.
Such as Fig. 8 and shown in Figure 9, the methanol separator 5 of thick methanol recovery system comprises lime set withdrawing can 510, scum dredger tank 530 and upright radiator 520, and liquid isolate outlet is arranged on the Lower Half of lime set withdrawing can 510; The outlet of scum dredger tank 530 gaseous state isolates is arranged on the top of scum dredger tank 530; Upright radiator 520 is connected with air cooler 4 and heat-eliminating medium feeding mechanism respectively, and is arranged side by side above lime set withdrawing can 510 with scum dredger tank 530, and lime set withdrawing can 510 is connected with upright radiator 520 and scum dredger tank 530 respectively.
Utilize above-mentioned methanol separator 5 to separate when generating gas, generate gas and enter the tube side of upright radiator 520 and the cooling of the heat-eliminating medium heat exchange in the shell side from top to bottom, the lime set that generation air cooling but produces falls in the lime set withdrawing can 510, non-condensable gas then enters lime set withdrawing can 510 tops, and upwards baffling leaves methanol separator 5 by the outlet of scum dredger tank 530 tops again.Wherein, water cooler adopts vertical structure, the wax that the reaction generation gas of high-voltage high-speed can get off condensation is blown off in lime set withdrawing can 510, reduces wax condensation postadhesion on upright radiator 520 tube side tube walls, thus the impact that alleviates widely wax heat exchanging effect; Be arranged side by side top structure form at the lime set withdrawing can for upright radiator 520 and scum dredger tank 530, non-condensable gas makes progress baffling when leaving methanol separator 5 by scum dredger tank 530 tops outlets, most lime sets fall in the lime set withdrawing can 510 because of gravity, and most of lime set obtains effective separation; And adopt the up and down structure formation of combination for upright radiator in the prior art and lime set withdrawing can, gaseous phase outlet is arranged on the lime set withdrawing can upper portion side wall of upright radiator below, this structure formation, part lime set and wax just have little time to fall toward contact and have been blown out the lime set withdrawing can by gas phase, it is serious that gas phase is carried drop, and non-condensable gas and drop can not effective separations.
The scum dredger tank 530 of above-mentioned methanol separator 5 is used for removing reaction and generates the drop that gas carries.Adopt this methanol separator 5 wax that reaction generates in the gas can be separated, avoided making wax behind downstream unit in traditional paraffin removal method, in case temperature reduces, the wax in the thick methyl alcohol will condense, and has influence on the normal production of downstream unit.In the prior art, upright radiator and lime set withdrawing can adopt the up and down structure formation of combination, and this structure formation, part lime set and wax just have little time to fall toward contact and blown out the lime set withdrawing can by gas phase, and gas phase is still carried more drop; This upright radiator 520 of the present utility model and scum dredger tank 530 are arranged side by side the structure formation at the top of lime set withdrawing can 510, so that carrying the amount that lime set and wax enter upstream device, gas phase greatly reduces, air-flow is by scum dredger tank 530 scum dredgers, the drop that carries is further removed by scum dredger, and gas phase is carried the lime set amount and further reduced.Such as Fig. 8 and shown in Figure 9, the upright radiator 520 of preferred above-mentioned methanol separator 5 is shell and tube cooler, the tubulation two ends of upright radiator 520 are connected with air cooler 4 and lime set withdrawing can 510 respectively, and the shell side of upright radiator 520 is connected with the heat-eliminating medium feeding mechanism.Carrying out heat exchange by the heat-eliminating medium that moves in shell side and the generation gas that moves in tubulation realizes the cooling that generates gas freeze-out thick methyl alcohol and wax.
As shown in Figure 8, the bottom of lime set withdrawing can 510 is provided with wax discharging port, and is connected with catalytic cracking system by wax discharging port; The filling shell periphery that is positioned at liquid isolate outlet below of lime set withdrawing can 510 is provided with well heater 512.Bottom at lime set withdrawing can 510 arranges wax discharging port, regularly wax is discharged system, and for fear of wax lime set withdrawing can 510 bottoms be attached to the bottom periphery well heater 512 is set, preferred electromagnetic heater or microwave heater, when wax is solidified, when being difficult for discharging, adopt heater heats that wax is melted, be conducive to the discharge of wax.The wax of discharging can be transported to catalytic cracking system and obtain more chemical products.
As shown in figure 10, the condenser 7 of thick methanol recovery system comprises shell-and tube condenser 710 and liquid collecting tank 720, the pneumatic outlet of recycle gas compressor 6 is connected with the tubulation of shell-and tube condenser 710, heat-eliminating medium feeding mechanism phase is connected with the shell side of condenser 7, liquid collecting tank 720 is arranged on the bottom of shell-and tube condenser 710, be connected with the tubulation of shell-and tube condenser 710, thick methyl alcohol outlet is arranged on the bottom of liquid collecting tank 720, and the circulation gas outlet is arranged on the top of liquid collecting tank 720.The thick methyl alcohol that obtains after the condensation is collected in the liquid collecting tank 720, and circulation gas enters in the liquid collecting tank 720 and then exports effusion liquid collecting tank 720 by the circulation gas that is arranged on liquid collecting tank 720 tops, carries out recycle.
As shown in Figure 3, the heat-eliminating medium feeding mechanism of thick methanol recovery system comprises recirculated water feeding mechanism and tempering air feeding mechanism, and the recirculated water feeding mechanism is connected with the shell side of upright radiator 520 and shell-and tube condenser 710; The tempering air feeding mechanism comprises room air line of pipes and ambient air line of pipes, and room air line of pipes and ambient air line of pipes are connected with the shell side of upright radiator 520 and shell-and tube condenser 710 respectively.
The amount of the heat-eliminating medium that thick system for methanol synthesis is required is very large, and the general recirculated water that adopts cools off at present, the utility model when adopting recirculated water with air as heat-eliminating medium, further reduced the cost of heat-eliminating medium.And, if temperature is low and differ larger than the temperature of system for methanol synthesis in the workshop of thick methanol recovery system, can adopts room air as heat-eliminating medium and adopt the room air line of pipes to carry; When room air can not meet the demands, can adopt ambient air as heat-eliminating medium and adopt the ambient air line of pipes to carry; Also can be with room air and ambient air gas mixture as heat-eliminating medium, regulate the heat-eliminating medium that room air and ambient air obtain to meet need of production, as: lower at the northern area winter temperature, directly with cold outdoor environment air, temperature is excessively low, may cause the damage of equipment, by with the cooling air that mixes to obtain the matters temperature of room air.Room air and ambient air preferably at first filter dust removal dust and part water through air filter in use, are then carried by the gas blower that is arranged on the pipeline; Be equipped with variable valve on room air line of pipes and the ambient air line of pipes, can adjust the tempering air temperature by the flow of regulating both.In addition, the consumption of circulation water and air can adopt control valve to regulate according to the actual requirements.
As shown in Figure 3, the reactive gas cleaning system of thick methanol recovery system comprises fresh synthesis gas compressor 8 and reactive gas cleaning groove 9, and fresh synthesis gas compressor 8 is connected with hydrogen recovery system and fresh reactant source of the gas by gas feed; Reactive gas cleaning groove 9 one ends are connected with the pneumatic outlet of fresh synthesis gas compressor 8, and the other end is connected with paste state bed reactor 1.
The above is preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any modification of doing, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (16)
1. a thick system for methanol synthesis is characterized in that, described thick system for methanol synthesis comprises:
Paste state bed reactor (1), reaction gas produces under catalyst action and generates gas in described paste state bed reactor (1);
Cyclonic separator (10), and have the letter shoot line of generation and catalyzer reflux pipeline between the described paste state bed reactor (1);
The inert solvent recovery system is arranged on the extension pipeline of the generation letter shoot line between described paste state bed reactor (1) and the described cyclonic separator (10), and and described paste state bed reactor (1) between have the inert solvent reflux pipeline;
Thick methanol recovery system, be connected with described inert solvent recovery system and process from the generation of described inert solvent recovery system and be so incensed that the thick methyl alcohol and the circulation gas that separate, and have the admission line that enters described paste state bed reactor (1) at least part of described circulation gas between described thick methanol recovery system and the described paste state bed reactor (1).
2. thick system for methanol synthesis according to claim 1 is characterized in that, described thick system for methanol synthesis also comprises:
Hydrogen recovery system, the hydrogen in the circulation gas that reclaims described thick methanol recovery system that is connected with described thick methanol recovery system;
The reactive gas cleaning system, the one end formation admission line that is connected with fresh reactant source of the gas and described hydrogen recovery system has the pipeline that enters described paste state bed reactor (1) for the fresh reactant gas after purifying and hydrogen between the other end and the described paste state bed reactor (1).
3. thick system for methanol synthesis according to claim 1 is characterized in that, described paste state bed reactor (1) comprising:
Bathing pool (100) is arranged on the top of described paste state bed reactor (1),
Have on the housing at described bathing pool (100) top to generate the gas outlet and export by described generation gas and be connected with described cyclonic separator (10);
Have the catalyzer refluxing opening that is connected with described cyclonic separator (10) and the inert solvent refluxing opening that is connected with described inert solvent recovery system on the sidewall (102) at described bathing pool (100) middle part;
Described bathing pool (100) bottom has the middle vertex of a cone towards the conical bottom wall of below;
Described bathing pool (100) inside is provided with gas distributor;
Gas buffer chamber (200) is arranged on the below of described bathing pool (100).
4. thick system for methanol synthesis according to claim 2 is characterized in that, the gas distributor in the described bathing pool (100) comprises:
Central airway (280) comprising:
Air inlet supervisor (281), an end is communicated with pipe connecting (630);
Be used for spraying a plurality of eddy flow jet pipes (282) of circumferential gyration airflow, one end communicates and circumferentially evenly arranging along described air inlet supervisor (281) with the perisporium that (281) are responsible in described air inlet, the other end is pneumatic outlet, and the pneumatic outlet of each described eddy flow jet pipe (282) extends along the oblique below of the central axis that departs from described air inlet supervisor (281);
Gas distribution tube group (620), centered by described central airway (280), be arranged on described central airway (280) around, have the ventilating pit (650) that communicates with the external world;
Pipe connecting (630) connects described central airway (280) and gas distribution tube group (620);
The gas distribution tube group (620) of described gas distributor is fixed on the sidewall (102) of described bathing pool (100), and the air inlet of described gas distributor supervisor (281) extends to the diapire (103) of described bathing pool (100).
5. thick system for methanol synthesis according to claim 3 is characterized in that,
Described gas distribution tube group (620) comprises at least two annular gas distribution pipes (622 that arrange with one heart, 623,624), described pipe connecting (630) is along the radially setting of described gas distribution tube group (620) and be communicated with each described annular gas distribution pipe (622,623,624), described ventilating pit (650) is distributed on the tube wall of each described annular gas distribution pipe (622,623,624), and the aperture arranges towards the below
Described ventilating pit (650) comprising:
The hole (652) of cutting sth. askew, the sidewall in the described hole of cutting sth. askew (652) along described gas distribution tube group (620) radially from inside to outside all to counterclockwise or all tilting to extend to clockwise direction;
The first straight hole (651), the sidewall of described the first straight hole (651) vertically extends, and described the first straight hole (651) is intervally arranged on each described annular gas distribution pipe (622,623,624) with the described hole of cutting sth. askew (652).
6. thick system for methanol synthesis according to claim 5, it is characterized in that, described gas distributor also comprises the side airway (380) that even number is communicated with described pipe connecting (630), described side airway (380) is arranged on two described annular gas distribution pipes (622 in twos symmetrically with respect to described central airway (280), 623,624) on the described pipe connecting (630) between, and with the equidirectional extension of described central airway (280).
7. thick system for methanol synthesis according to claim 5 is characterized in that, described pipe connecting (630) comprising:
The first pipe connecting (631), internal diameter along outermost annular gas distribution pipe (623) extends, pass described gas distribution tube (622,623,624) center is with each described annular gas distribution pipe (622,623,624) be communicated with, described central airway (280) is communicated with the center of described the first pipe connecting (631);
The second pipe connecting (632), vertical with described the first pipe connecting (631), and be arranged between outermost annular gas distribution pipe (623) and the most inboard annular gas distributed pipeline (622), with each described annular gas distribution pipe (622,623,624) be communicated with, described side airway (380) is communicated with described the second pipe connecting (632).
8. each described thick system for methanol synthesis in 7 according to claim 1 is characterized in that described inert solvent recovery system comprises:
Inert solvent condenser (2) is arranged on the extension pipeline of the generation letter shoot line between described paste state bed reactor (1) and the described cyclonic separator (10), and is connected with the pneumatic outlet of described cyclonic separator (10);
Drum (3), and have circulation line between the described inert solvent condenser (2).
9. thick system for methanol synthesis according to claim 8, it is characterized in that, described thick methanol recovery system comprises synthesis loop intermediate heat (12), air cooler (4), methanol separator (5), recycle gas compressor (6), condenser (7), circulating gas preheater (11), heat-eliminating medium feeding mechanism and thick methanol recovery device, described methanol separator (5) has liquid isolate outlet and the outlet of gaseous state isolate, described condenser (7) has thick methyl alcohol outlet and circulation gas outlet
Described inert solvent condenser (2), described synthesis loop intermediate heat (12), described air cooler (4) are connected successively with described methanol separator (5), and the described liquid isolate outlet of described methanol separator (5) is communicated with thick methyl alcohol the first recovery line of formation with described thick methanol recovery device;
The described gaseous state isolate outlet of described methanol separator (5) is connected with described recycle gas compressor (6), the pneumatic outlet of described recycle gas compressor (6) is connected with described condenser (7), the thick methyl alcohol outlet of described condenser (7) is communicated with described thick methanol recovery device, and the circulation gas outlet of described condenser (7) is connected with described paste state bed reactor (1) and described synthesis loop intermediate heat (12) is arranged in the circulation gas outlet and the pipeline between the described paste state bed reactor (1) of described condenser (7);
Described hydrogen recovery system is connected with pipeline between described methanol separator (5) and the described recycle gas compressor (6);
Described heat-eliminating medium feeding mechanism is connected with described methanol separator (5) and described condenser (7) respectively.
10. thick system for methanol synthesis according to claim 9, it is characterized in that, described thick methanol recovery system also comprises circulating gas preheater (11), be arranged in the circulation gas outlet and the pipeline between the described synthesis loop intermediate heat (12) of described condenser (7), and described circulating gas preheater (11) is connected with described drum (3).
11. thick system for methanol synthesis according to claim 9 is characterized in that, described methanol separator (5) comprising:
Lime set withdrawing can (510), described liquid isolate outlet is arranged on the Lower Half of described lime set withdrawing can (510);
Scum dredger tank (530), described gaseous state isolate outlet is arranged on the top of described scum dredger tank (530);
Upright radiator (520), be connected with described air cooler (4) and described heat-eliminating medium feeding mechanism respectively, and be arranged side by side in the top of described lime set withdrawing can (510) with described scum dredger tank (530), and described lime set withdrawing can (510) is connected with described upright radiator (520) and described scum dredger tank (530) respectively.
12. thick system for methanol synthesis according to claim 11, it is characterized in that, described upright radiator (520) is shell and tube cooler, the tubulation two ends of described upright radiator (520) are connected with described air cooler (4) and described lime set withdrawing can (510) respectively, and the shell side of described upright radiator (520) is connected with described heat-eliminating medium feeding mechanism.
13. thick system for methanol synthesis according to claim 11 is characterized in that, the bottom of described lime set withdrawing can (510) is provided with wax discharging port, and is connected with catalytic cracking system by described wax discharging port; The filling shell periphery that is positioned at described liquid isolate outlet below of described lime set withdrawing can (510) is provided with well heater (512).
14. thick system for methanol synthesis according to claim 11 is characterized in that, described condenser (7) comprising:
Shell-and tube condenser (710), the pneumatic outlet of described recycle gas compressor (6) is connected with the tubulation of described shell-and tube condenser (710), and described heat-eliminating medium feeding mechanism phase is connected with the shell side of described condenser (7),
Liquid collecting tank (720), be arranged on the bottom of described shell-and tube condenser (710), be connected with the tubulation of described shell-and tube condenser (710), described thick methyl alcohol outlet is arranged on the bottom of described liquid collecting tank (720), and described circulation gas outlet is arranged on the top of described liquid collecting tank (720).
15. thick system for methanol synthesis according to claim 14 is characterized in that, described heat-eliminating medium feeding mechanism comprises:
The recirculated water feeding mechanism is connected with the shell side of described upright radiator (520) and described shell-and tube condenser (710);
The tempering air feeding mechanism, comprise room air line of pipes and ambient air line of pipes, described room air line of pipes and described ambient air line of pipes are connected with the shell side of described upright radiator (520) and described shell-and tube condenser (710) respectively.
16. thick system for methanol synthesis according to claim 11 is characterized in that, described reactive gas cleaning system comprises:
Fresh synthesis gas compressor (8) is connected with described hydrogen recovery system and fresh reactant source of the gas by gas feed;
Reactive gas cleaning groove (9), an end is connected with the pneumatic outlet of described fresh synthesis gas compressor (8), and the other end is connected with described paste state bed reactor (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205055473U CN202808647U (en) | 2012-09-28 | 2012-09-28 | Crude methanol synthetic system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205055473U CN202808647U (en) | 2012-09-28 | 2012-09-28 | Crude methanol synthetic system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102850182A (en) * | 2012-09-28 | 2013-01-02 | 神华集团有限责任公司 | Coarse methanol synthesis system |
| CN103695043A (en) * | 2013-12-26 | 2014-04-02 | 上海国际化建工程咨询公司 | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof |
| CN104848737A (en) * | 2015-05-11 | 2015-08-19 | 神华集团有限责任公司 | Cleaning method of reactor overhead condenser |
-
2012
- 2012-09-28 CN CN2012205055473U patent/CN202808647U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102850182A (en) * | 2012-09-28 | 2013-01-02 | 神华集团有限责任公司 | Coarse methanol synthesis system |
| CN102850182B (en) * | 2012-09-28 | 2014-12-10 | 神华集团有限责任公司 | Coarse methanol synthesis system |
| CN103695043A (en) * | 2013-12-26 | 2014-04-02 | 上海国际化建工程咨询公司 | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof |
| CN104848737A (en) * | 2015-05-11 | 2015-08-19 | 神华集团有限责任公司 | Cleaning method of reactor overhead condenser |
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