CN204848758U - Remove bed methyl alcohol system hydrocarbon system all - Google Patents
Remove bed methyl alcohol system hydrocarbon system all Download PDFInfo
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- CN204848758U CN204848758U CN201520182709.8U CN201520182709U CN204848758U CN 204848758 U CN204848758 U CN 204848758U CN 201520182709 U CN201520182709 U CN 201520182709U CN 204848758 U CN204848758 U CN 204848758U
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Abstract
The utility model relates to a remove bed methyl alcohol system hydrocarbon system all, including hydrocarbon synthesis, separation and back processing unit, adopt the reactor of two at least mutual series connection among the hydrocarbon synthesis unit, reactant crosses each reactor with the contrary order direction flow of catalyst, the circulating air including the lower carbon number hydrocarbons that the separating element produced returns hydrocarbon synthesis unit's different feed entrance points, cold shock gas or raw materials make -gas as hydrocarbon synthesis unit, utilize raw materials methyl alcohol to wash the absorption to C1-C4 light component that the separating element produced, and return the feeding and change, thereby turn into methyl alcohol high added value's the lighter hydrocarbons of stabilizing that contain BTX aromatics. This system has gone on utilizing totally step by step to the activity of catalyst, has improved reaction sequence's the control that refines, has realized between the processing technology material utilization and heat integration effectively, has reduced environmental pollution when improve the product yield, reducing the energy consumption.
Description
Technical field
The utility model relates to a kind of Methanol hydrocarbon system adopting moving-bed.
Background technology
BTX aromatic hydrocarbons (Benzene, Toluene, Xylene) is the important basic raw material of petrochemical complex, and wherein p-Xylol (PX) demand is maximum.Along with the rapid expansion of domestic PX downstream PTA, production of polyester ability, on market, PX supplies wretched insufficiency, and to 2013, China's p-Xylol external dependence degree was up to 55.3%, and insufficiency of supply-demand strengthens further.Traditional technology production PX projects construction difficulty is large, production technology threshold is high, investment large, limits more by raw material naphtha resource.The increase that is nervous and consumers demand of current China's oil resource causes the shortage of resources such as raw material petroleum naphtha, solar oil of producing aromatic hydrocarbons, must seek new way and substitute traditional petroleum path production aromatic hydrocarbon product.What form sharp contrast therewith is domestic rich coal resources, is mainly that the methyl alcohol production capacity of raw material production is seriously superfluous with coal.In conjunction with the fundamental realities of the country of China's " oil starvation, weak breath, rich coal ", utilize abundant coal resources synthesizing methanol, research and development methanol oxidation transforms prepares aromatic hydrocarbons (MTA) technique, just high density PX can be obtained at production link, improve the added value of Downstream Products of Methanol, thus effectively reduce aromatic hydrocarbon product to the dependency of oil.
The aromatization of methanol technology of research and development both at home and abroad just progressively enters the industrialization stage at present, and portion of techniques realizes industrialization.MOBILE fixed bed Methanol aromatic hydrocarbons (gasoline processed) technology in 20th century the seventies achieve industrialization, and obtain industrial application at home; Shanxi coalification institute of Chinese Academy of Sciences bed technology obtained industrial application at home in 2010; Tsing-Hua University's fluidized-bed aromatization of methanol technology achieved ton industrial demonstration unit and runs in 2013.At present, fixed bed production technology range of application is comparatively wide, but is limited to the switching between reaction regeneration, and production capacity is restricted; Although fluidized-bed relies on the process of its successive reaction regeneration, production capacity has very large development space, the fluidization operation for this special material of methyl alcohol still needs to explore technique and operating method further.All there is certain shortcoming in current fixed bed and fluidized bed process mode, governs the extensive development in Methanol aromatic hydrocarbons field to some extent, specific as follows:
1) shortcoming of fixed bed operation mode:
(1) reaction regeneration frequently switches, and decaying catalyst needs to be interrupted regeneration, and reactor was significantly compressed for the time of reacting, production capacity critical constraints; (2) reaction regeneration frequently switches not only complex operation, and there is mishandle hidden danger, is unfavorable for long-term operation; (3) need for some time just can reach smooth running state by after regeneration incision reaction, material loss is larger; (4) general facilities consumption is large, and particularly reaction regeneration handoff procedure needs to consume a large amount of nitrogen; (5) easily there is the situation such as channel, bias current in production process in fixed bed, easily coking in reactor, and catalyzer duct easily blocks, and affects quality product and production safety; (6) fixed bed reaction heat removes difficulty, and catalyst change cost is high.
2) shortcoming of fluidized bed process mode:
(1) fluidized-bed layer inner catalyst back-mixing degree is heavier, and local reaction excessively easily causes coking; (2) in fluidized-bed layer, turbulence is violent, serious wear, and expensive catalyzer cracky and then generation are run and damaged, and cause loss economically; (3) in fluidized-bed layer, residence time destribution is comparatively wide, easily causes product slates wider, and the yield of target product reduces; (4) temperature and pressure surge all can affect the efficiency of gas solid separation system, and then affect subsequent fractionation system; (5) for the reactive system that coking yield is low, the reaction-regeneration system thermal equilibrium of fluidized-bed is difficult to maintain.
Summary of the invention
In order to overcome the above-mentioned defect under prior art, the purpose of this utility model is to provide a kind of moving-bed Methanol hydrocarbon system, this system can realize the serialization of aromatization of methanol reaction and catalyst regeneration process, the refinement controlling extent of reaction process can be improved, realizing between complete processing material effectively utilizes with heat integrated, the advantage such as have that catalyst activity is stable, pressure drop is low, plug flow reaction, back-mixing are few.
The technical solution of the utility model is:
A kind of moving-bed Methanol hydrocarbon system, comprise hydrocarbon synthesis unit, described hydrocarbon synthesis unit adopts the 1st reactor of multiple connection (being called series connection herein) successively to N reactor, N be more than or equal to 2 natural number, in adjacent two reactors, the catalyst outlet of last reactor connects the catalyst inlet of a rear reactor, the reacting product outlet of a rear reactor connects the material inlet of last reactor, the catalyst outlet of N reactor connects the import of a revivifier, the outlet of described revivifier connects the catalyst inlet of the 1st reactor, the material inlet of N reactor forms the material inlet of hydrocarbon synthesis unit, the reacting product outlet of the 1st reactor forms the reacting product outlet of hydrocarbon synthesis unit, described reactor is radially moving bed reactor.
Described reactor can be " π " type reactor or " Z " type reactor, can be to cardioid reactor or centrifugal type reactor.
Described moving-bed Methanol hydrocarbon system can also comprise separating unit and post-processing unit, described separating unit comprises gas-oil-water three-phase separating device and single-stage or multistage oil phase fractionation plant, the reacting product outlet of hydrocarbon synthesis unit connects the material inlet of three-phase separating device through reaction discharging pipeline, and pipeline is provided with refrigerating unit, the water out of three-phase separating device connects oil-contained waste water treatment device, the oil phase outlet of three-phase separating device connects the import of oil phase fractionation plant, the gaseous phase outlet of three-phase separating device connects two pipelines, article one, connect the import of post-processing unit, another connects the import of a compressor, the outlet of this compressor connects the material inlet of N reactor through wall scroll circulation gas pipeline, or connect through many articles of circulation gas pipeline correspondences the material inlet comprising multiple reactors of N reactor.
The material inlet of hydrocarbon synthesis unit connects methyl alcohol from tank field through supply lines, the upstream of supply lines is provided with fresh feed pump, described reaction discharging pipeline is preferably provided with many discharging branch lines, discharging branch line is provided with heat exchange unit separately, and separately as the turnover pipeline of corresponding heat exchange unit exothermic medium, the turnover pipeline of the heat-absorbing medium of at least one heat exchange unit is supply lines, the turnover pipeline of the heat-absorbing medium of other heat exchange units comprises circulation gas pipeline, and these heat exchange units are positioned at the upstream of refrigerating unit.
Described post-processing unit can adopt absorption tower, the upper and lower on absorption tower is respectively equipped with methanol solvate import and combi inlet port, the top on absorption tower and bottom are respectively equipped with precipitation matter pneumatic outlet and absorption liquid outlet, combi inlet port forms the import of post-processing unit, absorption liquid outlet preferably connects supply lines by the road, and tie point is positioned at the upstream of heat exchange unit in supply lines.
The oil phase fractionation plant of described single-stage can be depentanizer or separation column, the material inlet of tower forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of tower connects product storage tank, the gaseous phase outlet of return tank of top of the tower tank deck connects the import of post-processing unit, when oil phase fractionation plant is depentanizer, the export abroad of trim the top of column pump connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium; When oil phase fractionation plant is separation column, the export abroad auxiliary connection product storage tank of trim the top of column pump, or the material inlet of the 1st reactor is connected through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium.
Described multistage oil phase fractionation plant can comprise depentanizer and debutanizing tower, the material inlet of depentanizer forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of depentanizer tower connects product storage tank, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of depentanize tower top reflux pump connects the material inlet of debutanizing tower, liquid-phase outlet at the bottom of debutanizing tower tower connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of debutylize tower top reflux pump connects supply lines by the road, tie point is positioned at the upstream of heat exchange unit in supply lines.
Described multistage oil phase fractionation plant can comprise depentanizer and debutanizing tower, the material inlet of depentanizer forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of depentanizer tower connects product storage tank, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of depentanize tower top reflux pump connects the material inlet of debutanizing tower, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of debutylize tower top reflux pump can also connect the material inlet of dehydrogenation reactor, be connected the material inlet of the 1st reactor through return line after liquid-phase outlet pipeline at the bottom of debutanizing tower tower converges with the material outlet pipeline of dehydrogenation reactor, return line is provided with heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium.
For aforementioned multiple described moving-bed Methanol hydrocarbon system, described separating unit can also comprise de-liquefied gas tower, the outlet of described compressor also connects the material inlet of described de-liquefied gas tower through an additional circulation air pipe, de-liquid-phase outlet at the bottom of liquefied gas tower tower connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium; The gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck connects the import of post-processing unit, or, the gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck connects through circulation residue gas compressor, water cooler the material inlet taking off liquefied gas tower top knockout drum successively, the tank deck gaseous phase outlet of de-liquefied gas tower top knockout drum connects the import of post-processing unit, and at the bottom of the tank of de-liquefied gas tower top knockout drum, liquid-phase outlet accesses de-liquefied gas return tank of top of the tower by the road; The export abroad of de-liquefied gas trim the top of column pump connects liquefied gas product storage tank.
Should according to the above-mentioned suitable de-liquefied gas tower decoration form of actually operating pressure selection in practice, such as, when de-liquefied gas tower working pressure is higher, as 1.5MPaG, front a kind of decoration form should be selected, when de-liquefied gas tower working pressure is lower, as 0.4MPaG, rear a kind of decoration form should be selected, namely by supercharging condensation, secondary gas-liquid separation is carried out to the gas phase that de-liquefied gas return tank of top of the tower tank deck is discharged, good separating effect can be reached under ensureing various working pressure.
Described additional circulation air pipe can also be arranged residue gas compressor or by setting gradually the cold heat exchange unit of ammonia and topping-up pump before and after circulation gas flow direction.
For aforementioned moving-bed Methanol hydrocarbon system described in any one, in supply lines heat exchange unit and N reactor material inlet between pipeline section on be also preferably provided with at least one and be no more than N-1 feed branch line, the material outlet of feed branch line connects the material inlet of the part or all of reactor except N reactor one to one.
The beneficial effects of the utility model are:
1, adopt moving-bed to carry out aromatization of methanol, overcome the shortcomings such as fixed bed production capacity is low, pressure drop is large, catalyst life is short, the easy coking and blocking of bed; Overcome again the shortcomings such as fluidized-bed back-mixing degree is large, catalyzer is easy to wear, race damage.Utilize moving-bed successive reaction to regenerate, ensure that increasing substantially of production capacity; Be heated for methyl alcohol easily decompose, the feature of easily coking completely in the short period of time, utilize movable bed catalyst plug flow to move, the radial contact reacts of raw material, effectively ensure that methanol conversion and reaction degree of uniformity; Utilize the feature that radially moving bed pressure drop is low, effectively saved energy waste, catalyzer plug flow in bed moves down, two-phase transportation, and flow velocity is low, avoids the wearing and tearing of catalyzer, effectively controls the distribution of reaction product, improves the selectivity of target product.While guarantee methyl alcohol high conversion, improve product yield.
2, adopting the form of multiple reactors in series, flows in inverse order in reaction raw materials flow direction and catalyst motion direction.Fresh methanol is heated and is easily decomposed, first the least significant end reactor (i.e. N reactor) of arranged in series is entered, react with the catalyst exposure through its previous stage reactor pre-passivating, lower catalyst activity efficiently avoid methyl alcohol short period of time decomposes.React in least significant end reactor and generate the intermediates such as low-carbon (LC) hydro carbons based on methyl alcohol, methanol feedstock provides CH3-group in addition, also promotes aromatization of methanol, the alkylating generation of hydro carbons to a certain extent.Under lower catalytic type activity, reaction temperature and, reaction temperature rising is less, reaction be easy to control.Reaction intermediate enters most top reactor (i.e. the 1st reactor), with the high activated catalyst contact reacts from revivifier.Because catalyst activity is higher, effectively can be promoted based on the more difficult reaction carried out of aromatization of low carbon hydrocarbon, hydrocarbon restructuring etc., when part methanol feedstock enters most top reactor in addition, provided CH3-group, also promoted the degree that alkylation transforms.Therefore speed of reaction is very fast, and reaction efficiency is high, is conducive to the generation of aromatic hydrocarbons target product.
Temperature rise is there is larger relative to single reactor operation, operation controls the problems such as difficulty is larger, this technique adopts multiple reactors in series, reaction raw materials and catalyzer are against order direction flow pattern, utilize the feature that raw material reaction speed is different and different to catalyst activity sexual demand, efficiently avoid methyl alcohol and cross thermolysis, both carried out utilizing completely to the high low activity of catalyzer, carry out utilizing step by step to it according to reaction depth again, the refinement achieving reaction process controls, effectively control reaction temperature rising, the complexity that improve differential responses process mates adaptability with catalyst activity height, promote while being conducive to product purity and yield.
3, react discharging pipeline and many discharging branch lines are set, discharging branch line is provided with heat exchange unit separately, and using discharging branch line separately as the turnover pipeline of corresponding heat exchange unit exothermic medium, the feature that reaction product potential temperature is high, latent heat is large of each reactor can be made full use of, with its heat, one or many preheating is carried out to the circulation gas that reaction feed and product separation go out, efficiently utilize own heat and achieve the up to standard of reaction raw materials temperature, thus save outer heat supplied.
Adopt and reaction product is divided into multiply and the mode of difference preheated feed and circulation gas, can by regulating the throughput ratio of multiply logistics, flexible feeding temperature, makes feeding temperature and reaction temperature rising match.Thus make whole reaction have very strong regulating power and anti-fluctuation ability.This Energy Efficient that can realize is recycled, and the hot integration mode that can realize again flexible has saved energy effectively.
4, make the outlet of compressor connect through many articles of circulation gas pipelines correspondence the material inlet comprising multiple reactors of N reactor, be divided into by circulation gas multiply to return different reactors exactly, and return different reactors and play different effects.Preferably have in the application that two strands of circulation gas return the 1st respectively, N reactor, what play act as:
(1) circulation gas 1: return least significant end reactor, namely mix with fresh methanol charging 1, due in least significant end reactor to generate lower carbon number hydrocarbons intermediate product, aromatization of methanol, the CH3-group that C1 ~ C4 component in circulation gas can provide with methyl alcohol participates in reacting jointly, improve yield, promote that alkylation transforms.
(2) circulation gas 2: return most top reactor, namely mix with rear stage reactor product intermediates.Due in most top reactor with alkane aromatization, be reassembled as master, catalyst activity is high, and reaction is violent, and heat release is large, and therefore circulation gas plays cooling/cold shock effect to most top reactor, prevents from reacting too fast coking.Methyl alcohol in the alkane that C1 ~ C4 component in circulation gas and later separation part return and raw material 2 facilitates methanol alkylation and reacts, and is conducive to the generation promoting aromatic hydrocarbons, improves PX selectivity.
By regulating two strands of circulation gas flows, the reaction depth of adjustable most top reactor and least significant end reactor, enables the effectively relay of two reactor reactions, coupling, improves aromatics yield.
5, liquid-phase outlet at the bottom of the export abroad of depentanize tower top reflux pump in separating unit, debutanizing tower tower and the liquid-phase outlet at the bottom of de-liquefied gas tower tower connect the material inlet of the 1st reactor through return line, make C5 component return most top reactor feed, namely mix with rear stage reactor product intermediates.Because most top catalyst reactor activity is high, be swift in response, there is again CH3-group, the lighter hydrocarbons that C5 component and circulation gas return can generate aromatic hydrocarbons by aromatization rapidly in most top reactor, thus efficiently utilize the value of C5 byproduct, decrease whole device byproduct quantity, improve aromatics yield.
6, depentanize tower top light constituent C1 ~ C4 enters in an absorption tower, draws one methanol feeding 2 couples of C1 ~ C4 and carries out spray-absorption, effectively C3, C4 component in depentanizer top gas is absorbed and is dissolved in wherein from fresh methanol charging.This strand of material mixes with the charging entering least significant end reactor, namely mixes with fresh methanol charging 1, thus efficiently utilizes C3, C4 component, utilizes the solvability of raw material self, adds quantity and the diversity of raw material, decreases raw material consumption.This normal temperature methanol wash column mode can realize absorbing efficiently at normal temperatures, has both eliminated the reboiler of conventional fractionation tower height energy consumption, and the raw material that make use of again technique self, as absorbing medium, all has huge advantage with creative from energy-conservation with conservation aspect.
In addition, the non-condensable gas in depentanizer top gas washes out by normal temperature methanol wash column mode, the hydrogen-containing gas particularly in system, effectively prevent non-condensable gas gathering in systems in which.
7, the setting of debutanizing tower significantly reduces the load of depentanize tower top, and depentanize tower top condensing temperature only need higher than the boiling temperature of C2.C5 and C1 ~ C4 is separated by debutanizing tower, C5 component returns most top reactor feed, because most top catalyst reactor activity is high, be swift in response, there is again CH3-group, the lighter hydrocarbons that C5 component and circulation gas return can generate aromatic hydrocarbons by aromatization rapidly in most top reactor, thus efficiently utilize the value of C5 byproduct, decrease whole device byproduct quantity, improve aromatics yield.Tower top C1, C2 component and C3, C4 Component seperation, C1, C2 component and depentanizer C1, C2 component enter normal temperature methanol wash column absorption tower after converging.Debutanizing tower effectively reduces C3, C4 content entering absorption tower, decreases methanol usage, achieves the saving of raw material and the energy.
8, debutanizing tower is separated the C3 ~ C4 component obtained and is converted into C3, C4 unsaturated hydrocarbons by the setting of dehydrogenation reactor effectively, converge with C5 at the bottom of debutanizing tower tower, and then mix with intermediates, enter reactor 1, the C=C himself contained participates in reaction, participate in cyclisation, restructuring directly, add product yield.In addition, the setting of dehydrogenation reactor improves the hydrogen purity of methanol wash column absorption tower tower top non-condensable gas effectively, and high hydrogen purity is conducive to the separation of subsequent gases.
9, the gaseous phase outlet of three-phase separating device connects two pipelines, wherein one connects the import of post-processing unit, make one gas phase as the charging on normal temperature methanol wash column absorption tower, can in time by the hydrogen extraction in system, the hydrogen effectively reduced in system is assembled.
10, this process products only comprises stable light hydrocarbon containing BTX aromatics and small part non-condensable gas, does not produce liquefied gas, the whole recycle of byproduct, farthest achieves effective utilization of material.By the setting to separation column operating parameters, can the light aromatic hydrocarbons of by-product part C6, C7, according to the market conditions flexible adjusting device product category of aromatic hydrocarbon product kind.
11, can effectively be separated the liquefied gas in component loops gas, C1 ~ C2 light constituent, C5 component by arranging de-liquefied gas tower, here the C5 component obtained is converged with the C5 component obtained by depentanizer and is returned reaction feed, efficiently utilizes reaction by-product; C1 ~ C2 lightweight gas mixes with depentanizer top gas and carries out normal temperature methanol wash column, reclaims C3 ~ C4 further as reaction feed; C3 ~ C4 liquefied gas component that de-liquefied gas tower produces exports as handicraft product liquefied gas, has enriched the product category of this technique.
12, the cold heat exchange unit of ammonia arranged can when reaction pressure be lower, is effectively liquefied by circulation gas, then makes it reach to enter the condition of de-liquefied gas tower by supercharging, thus effectively from circulation gas, reclaims C3 ~ C4 component.
Accompanying drawing explanation
Fig. 1 is the sketch of first embodiment of the present utility model;
Fig. 2 is the sketch of second embodiment of the present utility model;
Fig. 3 is the sketch of the 3rd embodiment of the present utility model;
Fig. 4 is the sketch of the 4th embodiment of the present utility model;
Fig. 5 is the sketch of the 5th embodiment of the present utility model;
Fig. 6 is the sketch of the 6th embodiment of the present utility model;
Fig. 7 is the sketch of the 7th embodiment of the present utility model;
Fig. 8 is the sketch of the 8th embodiment of the present utility model.
Embodiment
The utility model provides a kind of moving-bed Methanol hydrocarbon system, comprise hydrocarbon synthesis unit, described hydrocarbon synthesis unit adopts multiple the 1st reactor connecting (being called series connection herein) successively, 2nd reactor, until N reactor, N be more than or equal to 2 natural number, in adjacent two reactors, the catalyst outlet of last reactor connects the catalyst inlet of a rear reactor, the reacting product outlet of a rear reactor connects the material inlet of last reactor, the catalyst outlet of N reactor connects the import of a revivifier, the outlet of described revivifier connects the catalyst inlet of the 1st reactor, the material inlet of N reactor forms the material inlet of hydrocarbon synthesis unit, the reacting product outlet of the 1st reactor forms the reacting product outlet of hydrocarbon synthesis unit.Under above-mentioned reactor mode of connection, reaction raw materials and catalyzer flow through each reactor against order.Described reactor is radially moving bed reactor.Described reactor can be " π " type reactor or " Z " type reactor, can be to cardioid reactor or centrifugal type reactor.For Fig. 1, reaction process is: first fresh methanol charging 1 enters the 2nd reactor after heating up with reaction product heat exchange, with carry out radially moving bed contact reacts from the 1st reactor through the catalyzer of pre-passivating and generate intermediates, after catalyzer leaves the 2nd reactor, be promoted to regenerator overhead, fall in revivifier and regenerate, high activated catalyst after regeneration is promoted to the 1st reactor head, enter the 1st reactor after 2nd reactor product intermediates leave, carry out radially moving bed contact reacts with the high activated catalyst from revivifier.
Described moving-bed Methanol hydrocarbon system can also comprise separating unit and post-processing unit, described separating unit is used for carrying out separation and Extraction to the product of described hydrocarbon synthesis unit, comprise gas-oil-water three-phase separating device and single-stage or multistage oil phase fractionation plant, the reacting product outlet of hydrocarbon synthesis unit connects the material inlet of three-phase separating device through reaction discharging pipeline, and pipeline is provided with refrigerating unit, this refrigerating unit is for ensureing that the reaction product of hydrocarbon synthesis unit is cooled to the temperature be suitable for before entering three-phase separating device, such as be cooled to 40 ~ 60 DEG C, to meet the temperature condition of three phase separation.The water out of three-phase separating device connects oil-contained waste water treatment device, also can direct reuse to upstream coal gasification apparatus, thus effectively save general facilities.The oil phase outlet of three-phase separating device connects the import of oil phase fractionation plant, the liquid phase C6 that fractionation obtains ~ C10 component or C8 ~ C10 component are drawn as product, correspondingly, liquid phase C3 ~ C5 component or C3 ~ C7 component return hydrocarbon synthesis unit as reaction raw materials, converge respectively with different reactor charging; All the other light constituents enter post-processing unit as pending material.The gaseous phase outlet of three-phase separating device connects two pipelines, article one, connect the import of post-processing unit, shunting small part gas phase, another connects the import of a compressor, shunt most of gas phase, the outlet of this compressor connects the material inlet of N reactor through wall scroll circulation gas pipeline, or connects through many articles of circulation gas pipeline correspondences the material inlet comprising multiple reactors of N reactor, thus by regulating the reaction depth of each stock circulation gas Flow-rate adjustment respective reaction device.This compressor is used for being pressurized to 0.25 ~ 1.9MPaG to gas phase.Outlet for this compressor connects the situation of many circulation gas pipelines, is preferably 2 circulation gas pipelines, connects the material inlet of the 1st reactor and N reactor respectively.
The material inlet of hydrocarbon synthesis unit connects methyl alcohol from tank field through supply lines, and the upstream of supply lines is provided with fresh feed pump, and fresh methanol charging 1, through fresh feed pump pumping, boosts to 0.2 ~ 1.8MPaG, and temperature is 25 ~ 40 DEG C.Described reaction discharging pipeline is preferably provided with many discharging branch lines, discharging branch line is provided with heat exchange unit separately, as the 1st, 2, 3, 5 heat exchange units, and separately as the turnover pipeline of corresponding heat exchange unit exothermic medium, different stock reaction product 1, 2, 3, 4, 5 respectively as the exothermic medium of various heat exchange unit, the turnover pipeline of at least one heat exchange unit such as heat-absorbing medium of the 1st heat exchange unit is supply lines, the charging of hydrocarbon synthesis unit first carries out preheating as heat-absorbing medium, the turnover pipeline of the heat-absorbing medium of other heat exchange units comprises circulation gas pipeline, corresponding heat-absorbing medium is circulation gas, such as circulation gas 1, 2, certain heat exchange unit here also may be used for the intermediate product for later separation step, the heating of by product etc., these heat exchange units are preferably placed at the upstream of refrigerating unit, namely each stock reaction product is converged unification again and is entered refrigerating unit and cool further after heat exchange unit heat release cooling, until meet the temperature condition of three phase separation.The type of cooling of refrigerating unit can be the combination of dry type air cooling, wet type air cooling, water-cooled or aforesaid way.
Described post-processing unit can adopt absorption tower, the upper and lower on absorption tower is respectively equipped with methanol solvate import and combi inlet port, the top on absorption tower and bottom are respectively equipped with precipitation matter pneumatic outlet and absorption liquid outlet, combi inlet port forms the import of post-processing unit, absorption liquid outlet preferably connects supply lines by the road, and tie point is positioned at the upstream of heat exchange unit in supply lines.When post-processing unit runs, methanol feeding 2 enters absorption tower from methanol solvate import, from top to down to enter from combi inlet port and the pending material risen (mainly C1 ~ C2 and/or C1 ~ C4) carry out reverse normal temperature (such as 25 DEG C) spray, liquid at the bottom of absorption tower leaves absorption liquid outlet and converges along pipeline and methanol feeding 1, enters N reactor after together heating up with methanol feeding 1; Absorb tower top non-condensable gas (mainly C1, C2) to be discharged by precipitation matter pneumatic outlet, enter bleed-off system to use as fuel gas, or enter methanol-water cleaning device in order to reclaim methyl alcohol, the methyl alcohol of recovery can reuse to upstream coal gasification apparatus, also can be used as combustion gas.In absorption tower, methyl alcohol spray flow and bottom gas phase rising throughput ratio are 5 ~ 20, and service temperature is normal temperature, and pressure is 0.3 ~ 1.4MPaG.
The oil phase fractionation plant of described single-stage can be depentanizer (see Fig. 1,5,6,7,8) or separation column (see Fig. 4), and the tower top pressure of depentanizer is 0.3 ~ 1.75MPaG, and tower reactor pressure is 0.35 ~ 1.8MPaG; The tower top pressure of separation column is 0.06 ~ 1.6MPaG, and tower reactor pressure is 0.07 ~ 1.8MpaG.The material inlet of tower forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of tower connects product storage tank, for extraction C6 ~ C10 (for depentanizer) or C8 ~ C10 (for separation column), top gaseous phase is through dry type air cooling, wet type air cooling, the combination type of cooling cooling of water-cooled or aforesaid way, between the boiling point that temperature is down to C4 and C5 under logistics current pressure (for depentanizer) or C5 and C6 boiling point between (for separation column), enter return tank of top of the tower, the gaseous phase outlet of return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C4 mixture (for depentanizer) or C1 ~ C5 mixture (for separation column), when oil phase fractionation plant is depentanizer, C5 liquid phase is through the supercharging of trim the top of column pump, part backflow returns tower top, the material inlet that another part connects the 1st reactor by the export abroad of trim the top of column pump through return line enters the 1st reactor participation reaction, for C5 liquid phase is returned hydrocarbon synthesis unit, return line is provided with the 5th heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, and the reaction product with hydrocarbon synthesis unit carries out heat exchange intensification, when oil phase fractionation plant is separation column, C6 ~ C7 liquid phase is through the supercharging of trim the top of column pump, and part backflow returns tower top, another part is by export abroad auxiliary connection product storage tank extraction byproduct C6 ~ C7 liquid phase of trim the top of column pump, or also can return 1st reactor through return line as reaction raw materials with the same during employing depentanizer, and first on return line, carry out heat exchange intensification by the 5th heat exchange unit with the reaction product of hydrocarbon synthesis unit.
As shown in Figure 2, described multistage oil phase fractionation plant can comprise depentanizer and debutanizing tower, depentanizer tower top pressure is 0.3 ~ 1.75MPaG, tower reactor pressure is 0.35 ~ 1.8MPaG, debutanizing tower tower top pressure is 0.4 ~ 1.6MPaG, tower reactor pressure is 0.45 ~ 1.65MPaG, the material inlet of depentanizer forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of depentanizer tower connects product storage tank, for extraction aromatic hydrocarbon product C6 ~ C10, depentanizer top gaseous phase is through dry type air cooling, wet type air cooling, the combination type of cooling cooling of water-cooled or aforesaid way, when depentanizer working pressure is higher, cooling makes temperature be down between the boiling point of C2 and C3 under logistics current pressure, enter depentanize return tank of top of the tower, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C2 gaseous component, C3 ~ C5 liquid phase is through the supercharging of depentanize tower top reflux pump, part backflow returns depentanizer tower top, the material inlet that another part connects debutanizing tower by the export abroad of depentanize tower top reflux pump enters debutanizing tower, when depentanizer working pressure is lower, cooling makes temperature be reduced between the boiling point of C4 and C5 under logistics current pressure, enter depentanize return tank of top of the tower, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C4 gaseous component, C5 (usually also containing a small amount of C1 ~ C4) liquid phase is through the supercharging of depentanize tower top reflux pump, part backflow returns depentanizer tower top, and the material inlet that another part connects debutanizing tower by the export abroad of depentanize tower top reflux pump enters debutanizing tower.Liquid-phase outlet at the bottom of debutanizing tower tower connects the material inlet of the 1st reactor through return line, for liquid phase C5 is returned hydrocarbon synthesis unit, return line is provided with the 5th heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, and this heat exchange unit realizes heat exchange using the reaction product of hydrocarbon synthesis unit or external heat source as exothermic medium.Debutanizing tower top gaseous phase is through dry type air cooling, wet type air cooling, the combination type of cooling cooling of water-cooled or aforesaid way, when debutanizing tower working pressure is higher, cooling makes temperature be down between the boiling point of C2 and C3 under logistics current pressure, enter debutylize return tank of top of the tower, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C2 mixture, C3 ~ C4 liquid phase is through the supercharging of debutylize tower top reflux pump, part backflow returns debutanizing tower tower top, another part connects supply lines by the road by the export abroad of debutylize tower top reflux pump and returns hydrocarbon synthesis unit participation reaction, when debutanizing tower working pressure is lower, cooling makes temperature be down between the boiling point of C3 and C4 under logistics current pressure, enter debutylize return tank of top of the tower, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C3 mixture, C4 (usually containing a small amount of C3) liquid phase is through the supercharging of debutylize tower top reflux pump, part backflow returns debutanizing tower tower top, and another part connects supply lines by the road by the export abroad of debutylize tower top reflux pump and returns hydrocarbon synthesis unit participation reaction.The export abroad of debutylize tower top reflux pump is positioned at the upstream of heat exchange unit in supply lines with the tie point of supply lines by the road, makes C3, the C4 returned together enter the 1st heat exchange unit with methanol feeding 1 and heats up.
As shown in Figure 3, described multistage oil phase fractionation plant can comprise depentanizer and debutanizing tower, be connected the material inlet of dehydrogenation reactor with the export abroad of the multistage oil phase fractionation plant shown in Fig. 2 unlike debutylize tower top reflux pump thus make the C3 that debutylize tower top reflux pump pumps, C4 liquid phase enters dehydrogenation reactor dehydrogenation, the material outlet pipeline of liquid-phase outlet pipeline at the bottom of debutanizing tower tower (for discharging liquid phase C5) and dehydrogenation reactor is (for the C3 obtained after discharging dehydrogenation, C4 unsaturated hydrocarbons) converge after connect the material inlet of the 1st reactor through return line, for above-mentioned material is returned hydrocarbon synthesis unit, return line is provided with the 5th heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, C5 and C3 after intensification, C4 unsaturated hydrocarbons enters the 1st reactor and participates in reaction.Preferably arrange the 4th heat exchange unit before dehydrogenation reactor, for the C3 ~ C4 liquid phase before dehydrogenation is warming up to 350 ~ 540 DEG C, intensification thermal source is the reaction product of each reactor or outer supplying heat source.
For aforementioned multiple described moving-bed Methanol hydrocarbon system, described separating unit can also comprise de-liquefied gas tower, as Fig. 5, 6, 7, shown in 8, the outlet of described compressor also connects the material inlet of described de-liquefied gas tower through an additional circulation air pipe (for distributing circulation gas 3), the tower top pressure of de-liquefied gas tower is 0.3 ~ 1.6MPaG, tower reactor pressure is 0.35 ~ 1.65MPaG, de-liquid-phase outlet at the bottom of liquefied gas tower tower connects the material inlet of the 1st reactor through return line, for liquid phase C5 is returned hydrocarbon synthesis unit, return line is provided with heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, exothermic medium adopts the reaction product of external heat source or hydrocarbon synthesis unit, C5 enters the 1st reactor and participates in reaction after heating up.Heat exchange unit on the return line that heat exchange unit on the return line that de-liquefied gas tower is drawn and pipeline can be drawn with liquid phase fractionation plant and pipeline shares set of device.When de-liquefied gas tower working pressure is higher, should adopt shown in Fig. 5,6,7 and arrange, de-liquefied gas top gaseous phase cools through the combination type of cooling of dry type air cooling, wet type air cooling, water-cooled or aforesaid way, temperature is down between the boiling point of C2 and C3 under logistics current pressure, enter return tank of top of the tower, the gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck connects the import of post-processing unit, for discharging C1 ~ C2 mixture, carry out Recovery Purifying, C3 ~ C4 liquid phase is through the supercharging of trim the top of column pump, and part backflow returns tower top; Another part connects liquefied gas product storage tank by the export abroad of de-liquefied gas trim the top of column pump and realizes liquefied gas products C 3, C4 extraction.When de-liquefied gas tower working pressure is lower, should adopt shown in Fig. 8 and arrange, de-liquefied gas top gaseous phase is through dry type air cooling, wet type air cooling, the combination type of cooling cooling of water-cooled or aforesaid way, temperature is down between the boiling point of C3 and C4 under logistics current pressure, enter return tank of top of the tower, the gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck is successively through circulation residue gas compressor, water cooler connects the material inlet of de-liquefied gas tower top knockout drum, the first supercharging of the gas phase C1 ~ C3 condensation again of de-liquefied gas return tank of top of the tower tank deck, in de-liquefied gas tower top knockout drum, gas-liquid separation becomes gas phase C1 ~ C2 and liquid phase C3, wherein gas phase sends into post-processing unit, carry out Recovery Purifying, C3 liquid phase is back to de-liquefied gas return tank of top of the tower by the road and C4 converges, C3 ~ C4 liquid phase is through the supercharging of trim the top of column pump, part backflow returns tower top, another part connects liquefied gas product storage tank by the export abroad of de-liquefied gas trim the top of column pump and realizes liquefied gas products C 3, C4 extraction.
Described additional circulation air pipe can also arrange residue gas compressor, or by setting gradually the cold heat exchange unit of ammonia and topping-up pump before and after circulation gas flow direction.Arrange residue gas compressor, circulation gas is pressurized to 0.5 ~ 1.8MPaG; Arrange the cold heat exchange unit of ammonia and topping-up pump, circulation gas is first cooled to-13 ~ 30 DEG C through the cold heat exchange unit of ammonia, then is pressurized to 0.5 ~ 1.8MPaG through pump.
As shown in Fig. 3,4,6,7, pipeline section in the supply lines of described moving-bed Methanol hydrocarbon system between heat exchange unit (i.e. illustrated 1st heat exchange unit) and the material inlet of N reactor is also preferably provided with at least one and is no more than N-1 feed branch line, the material outlet of feed branch line connects the material inlet of the part or all of reactor except N reactor one to one.In Fig. 3,6, feed branch line is used for supplying raw material 1 to the 1st reactor, and raw material 2 enters the 2nd reactor through feed main line and participates in reaction; In Fig. 4,7, feed branch line is respectively used to the 1st, 2 reactors supply raw material 1,2, and raw material 3 enters the 3rd reactor through feed main line and participates in reaction.The major part of methanol feeding 1 enters N reactor by feed main line.
The alkane such as methyl alcohol directly adds reactor, can be reaction and provides CH3-group, the C5 that the LPG returned with circulation gas, later separation part return carry out the reaction such as alkane aromatization, methanol alkylation, promote the carrying out of aromatization, are conducive to improving aromatics yield.
The gas phase entering post-processing unit by different pipeline first can be converged and introduces post-processing unit together again.Return line for connecting the material inlet of the 1st reactor in separating unit can be connected by converging with the reacting product outlet pipeline of the 2nd reactor the material inlet realized with the 1st reactor.
The utility model can adopt following optimizing technology parameters scope to run: the liquid hourly space velocity in each reactor is preferably 1 ~ 5h
-1, the regeneration temperature of revivifier is 500 ~ 650 DEG C, regeneration pressure is 0.2 ~ 1.9MPaG, the pressure at most top reactor (i.e. the 1st reactor) is 0.20 ~ 1.73MPaG, temperature is 370 ~ 550 DEG C, the pressure of least significant end reactor (i.e. N reactor) is 0.25 ~ 1.75MPaG, temperature is 320 ~ 520 DEG C, often in adjacent two reactors the top pressure of last reactor not higher than the top pressure of a rear reactor, and all not higher than the top pressure of least significant end reactor, the minimal pressure of last reactor is not higher than the minimal pressure of a rear reactor, and all not higher than the minimal pressure of least significant end reactor.
Each heat exchange unit place can adopt the interchanger of one or more serial or parallel connections, and its thermal source can be the reaction product of certain reactor, also can be outer supplying heat source.The temperature elevating range at each heat exchange unit place is preferably: sub-thread circulation gas (as shown in Figure 1) is warming up to 320 ~ 480 DEG C by the 2nd heat exchange unit; During multiply circulation gas (as illustrated in figs. 2 through 8), the circulation gas entering most top reactor is warming up to 250 ~ 480 DEG C by the 3rd heat exchange unit, the circulation gas entering least significant end reactor is warming up to 320 ~ 480 DEG C by the 2nd heat exchange unit, methanol feedstock is warming up to 250 ~ 480 DEG C by the 1st heat exchange unit, the material that separating unit returns hydrocarbon synthesis unit is warming up to 150 ~ 250 DEG C through the 5th heat exchange unit, and C3, C4 before dehydrogenation are warming up to 350 ~ 540 DEG C by the 4th heat exchange unit.
Below that the principal feature of accompanying drawing 1-8 is illustrated:
Fig. 1 is containing the 1st, the 2 two reactor, and separating unit adopts depentanizer fractionation;
Fig. 2 is containing the 1st, the 2 two reactor, and separating unit adopts depentanizer, the fractionation of debutanizing tower two-stage;
Fig. 3 is containing the 1st, the 2 two reactor, and separating unit adopts depentanizer, the fractionation of debutanizing tower two-stage, and adopts dehydrogenation reactor to C3 ~ C4 dehydrogenation, and methanol feedstock divides 2 stocks not enter two reactors;
Fig. 4 is containing the 1st, the 2nd, the 3 three reactor, and separating unit adopts the fractionation of separation column single-stage, and methanol feedstock divides 3 stocks not enter three reactors;
Fig. 5 is containing the 1st, the 2 two reactor, and separating step adopts depentanizer and the fractionation of de-liquefied gas tower;
Fig. 6 is containing the 1st, the 2 two reactor, and separating step adopts depentanizer and the fractionation of de-liquefied gas tower, and circulation gas 3 is first through the cold heat exchange of ammonia and pump supercharging before entering de-liquefied gas tower, and methanol feedstock divides 2 stocks not enter two reactors;
Fig. 7 is containing the 1st, the 2nd, the 3 three reactor, and separating step adopts depentanizer and the fractionation of de-liquefied gas tower, and circulation gas 3 is first through residue gas compressor supercharging before entering de-liquefied gas tower, and methanol feedstock divides 3 stocks not enter three reactors;
Fig. 8 is containing the 1st, the 2 two reactor, and separating step adopts depentanizer and the fractionation of de-liquefied gas tower, the de-liquefied gas return tank of top of the tower tank deck gas phase of discharging again after compressed, cooling gas-liquid separation become gas-liquid two-phase, liquid phase returns de-liquefied gas return tank of top of the tower.
The utility model changes traditional single reaction vessel the form of more than 2 reactors in series into, utilize the feature that raw material reaction speed is different and different to catalyst activity sexual demand, efficiently avoid methyl alcohol and cross thermolysis, violent reaction process be divided into and severally comparatively leniently react, the relay that is coupled successively is carried out.Both carried out utilizing completely to the high low activity of catalyzer, and carried out subdivision utilization again according to reaction depth to it, the refinement achieving reaction process controls, and effectively controls reaction temperature rising, promotes while being conducive to product purity and yield.Efficiently solve traditional single reaction vessel and operate the problems such as the temperature rise existed is comparatively large, operation control difficulty is larger.
Separating unit is separated the C3 ~ C5 liquid-phase product obtained and turns back to reaction member participation reaction.Circulation gas returns and carries a large amount of CH3-groups, can react rapidly generation aromatic hydrocarbons, thus efficiently utilize the value of C5 byproduct in C5 Returning reactor, decreases whole device byproduct quantity.In C3 ~ C4 component Returning reactor, efficiently utilize C3, C4 component, effectively reduce raw material consumption, decrease the consumption of byproduct.
Claims (12)
1. a moving-bed Methanol hydrocarbon system, comprise hydrocarbon synthesis unit, it is characterized in that described hydrocarbon synthesis unit adopts multiple the 1st reactor connected successively to N reactor, N be more than or equal to 2 natural number, in adjacent two reactors, the catalyst outlet of last reactor connects the catalyst inlet of a rear reactor, the reacting product outlet of a rear reactor connects the material inlet of last reactor, the catalyst outlet of N reactor connects the import of a revivifier, the outlet of described revivifier connects the catalyst inlet of the 1st reactor, the material inlet of N reactor forms the material inlet of hydrocarbon synthesis unit, the reacting product outlet of the 1st reactor forms the reacting product outlet of hydrocarbon synthesis unit, described reactor is radially moving bed reactor.
2. moving-bed Methanol hydrocarbon system as claimed in claim 1, characterized by further comprising separating unit and post-processing unit, described separating unit comprises gas-oil-water three-phase separating device and single-stage or multistage oil phase fractionation plant, the reacting product outlet of hydrocarbon synthesis unit connects the material inlet of three-phase separating device through reaction discharging pipeline, and pipeline is provided with refrigerating unit, the water out of three-phase separating device connects oil-contained waste water treatment device, the oil phase outlet of three-phase separating device connects the import of oil phase fractionation plant, the gaseous phase outlet of three-phase separating device connects two pipelines, article one, connect the import of post-processing unit, another connects the import of a compressor, the outlet of this compressor connects the material inlet of N reactor through wall scroll circulation gas pipeline, or connect through many articles of circulation gas pipeline correspondences the material inlet comprising multiple reactors of N reactor.
3. moving-bed Methanol hydrocarbon system as claimed in claim 2, it is characterized in that the material inlet of hydrocarbon synthesis unit connects methyl alcohol from tank field through supply lines, the upstream of supply lines is provided with fresh feed pump, described reaction discharging pipeline is provided with many discharging branch lines, discharging branch line is provided with heat exchange unit separately, and separately as the turnover pipeline of corresponding heat exchange unit exothermic medium, the turnover pipeline of the heat-absorbing medium of at least one heat exchange unit is supply lines, the turnover pipeline of the heat-absorbing medium of other heat exchange units comprises circulation gas pipeline, these heat exchange units are positioned at the upstream of refrigerating unit.
4. moving-bed Methanol hydrocarbon system as claimed in claim 3, it is characterized in that described post-processing unit adopts absorption tower, the upper and lower on absorption tower is respectively equipped with methanol solvate import and combi inlet port, the top on absorption tower and bottom are respectively equipped with precipitation matter pneumatic outlet and absorption liquid outlet, combi inlet port forms the import of post-processing unit, absorption liquid outlet connects supply lines by the road, and tie point is positioned at the upstream of heat exchange unit in supply lines.
5. moving-bed Methanol hydrocarbon system as claimed in claim 4, it is characterized in that the oil phase fractionation plant of described single-stage is depentanizer or separation column, the material inlet of tower forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of tower connects product storage tank, the gaseous phase outlet of return tank of top of the tower tank deck connects the import of post-processing unit, when oil phase fractionation plant is depentanizer, the export abroad of trim the top of column pump connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium; When oil phase fractionation plant is separation column, the export abroad auxiliary connection product storage tank of trim the top of column pump, or the material inlet of the 1st reactor is connected through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium.
6. moving-bed Methanol hydrocarbon system as claimed in claim 4, it is characterized in that described multistage oil phase fractionation plant comprises depentanizer and debutanizing tower, the material inlet of depentanizer forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of depentanizer tower connects product storage tank, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of depentanize tower top reflux pump connects the material inlet of debutanizing tower, liquid-phase outlet at the bottom of debutanizing tower tower connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of debutylize tower top reflux pump connects supply lines by the road, tie point is positioned at the upstream of heat exchange unit in supply lines.
7. moving-bed Methanol hydrocarbon system as claimed in claim 4, it is characterized in that described multistage oil phase fractionation plant comprises depentanizer and debutanizing tower, the material inlet of depentanizer forms the import of oil phase fractionation plant, liquid-phase outlet at the bottom of depentanizer tower connects product storage tank, the gaseous phase outlet of depentanize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of depentanize tower top reflux pump connects the material inlet of debutanizing tower, the gaseous phase outlet of debutylize return tank of top of the tower tank deck connects the import of post-processing unit, the export abroad of debutylize tower top reflux pump connects the material inlet of dehydrogenation reactor, be connected the material inlet of the 1st reactor through return line after liquid-phase outlet pipeline at the bottom of debutanizing tower tower converges with the material outlet pipeline of dehydrogenation reactor, return line is provided with heat exchange unit, return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium.
8. the moving-bed Methanol hydrocarbon system as described in claim 2,3,4,5,6 or 7, it is characterized in that described separating unit also comprises de-liquefied gas tower, the outlet of described compressor also connects the material inlet of described de-liquefied gas tower through an additional circulation air pipe, de-liquid-phase outlet at the bottom of liquefied gas tower tower connects the material inlet of the 1st reactor through return line, return line is provided with heat exchange unit, and return line is as the turnover pipeline of this heat exchange unit heat-absorbing medium; The gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck connects the import of post-processing unit, or, the gaseous phase outlet of de-liquefied gas return tank of top of the tower tank deck connects through circulation residue gas compressor, water cooler the material inlet taking off liquefied gas tower top knockout drum successively, the tank deck gaseous phase outlet of de-liquefied gas tower top knockout drum connects the import of post-processing unit, and at the bottom of the tank of de-liquefied gas tower top knockout drum, liquid-phase outlet accesses de-liquefied gas return tank of top of the tower by the road; The export abroad of de-liquefied gas trim the top of column pump connects liquefied gas product storage tank.
9. moving-bed Methanol hydrocarbon system as claimed in claim 8, is characterized in that described additional circulation air pipe being arranged residue gas compressor or by setting gradually the cold heat exchange unit of ammonia and topping-up pump before and after circulation gas flow direction.
10. as the moving-bed Methanol hydrocarbon system in claim 3-7 as described in any one, pipeline section between the material inlet that it is characterized in that heat exchange unit and N reactor in supply lines is also provided with at least one and is no more than N-1 feed branch line, the material outlet of feed branch line connects the material inlet of the part or all of reactor except N reactor one to one.
11. moving-bed Methanol hydrocarbon systems as claimed in claim 8, pipeline section between the material inlet that it is characterized in that heat exchange unit and N reactor in supply lines is also provided with at least one and is no more than N-1 feed branch line, the material outlet of feed branch line connects the material inlet of the part or all of reactor except N reactor one to one.
12. moving-bed Methanol hydrocarbon systems as claimed in claim 9, pipeline section between the material inlet that it is characterized in that heat exchange unit and N reactor in supply lines is also provided with at least one and is no more than N-1 feed branch line, the material outlet of feed branch line connects the material inlet of the part or all of reactor except N reactor one to one.
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| CN201520182709.8U CN204848758U (en) | 2015-03-27 | 2015-03-27 | Remove bed methyl alcohol system hydrocarbon system all |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010642A (en) * | 2016-05-27 | 2016-10-12 | 山东东方宏业化工有限公司 | Device system for refining dry gas from methyl alcohol |
| CN107987907A (en) * | 2016-10-26 | 2018-05-04 | 中国石油天然气股份有限公司 | It is a kind of that the method rich in methane gas is prepared by synthesis gas |
-
2015
- 2015-03-27 CN CN201520182709.8U patent/CN204848758U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010642A (en) * | 2016-05-27 | 2016-10-12 | 山东东方宏业化工有限公司 | Device system for refining dry gas from methyl alcohol |
| CN107987907A (en) * | 2016-10-26 | 2018-05-04 | 中国石油天然气股份有限公司 | It is a kind of that the method rich in methane gas is prepared by synthesis gas |
| CN107987907B (en) * | 2016-10-26 | 2020-07-10 | 中国石油天然气股份有限公司 | Method for preparing methane-rich gas from synthesis gas |
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Address after: 100037 Beijing city Haidian District Zengguang Road No. 21 Patentee after: CHINA KUNLUN CONTRACTING & ENGINEERING Corp. Patentee after: China Textile Industry Design Institute Address before: 100037 Beijing city Haidian District Zengguang Road No. 21 Patentee before: CHINA KUNLUN CONTRACTING & ENGINEERING Corp. Patentee before: China Textile Industry Design Institute |
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Effective date of registration: 20170306 Address after: 100037 Beijing city Haidian District Zengguang Road No. 21 Patentee after: CHINA KUNLUN CONTRACTING & ENGINEERING Corp. Address before: 100037 Beijing city Haidian District Zengguang Road No. 21 Patentee before: CHINA KUNLUN CONTRACTING & ENGINEERING Corp. Patentee before: China Textile Industry Design Institute |