CN205076817U - Heat accumulation formula carbide production technology coproduction vinyl acetate's device - Google Patents
Heat accumulation formula carbide production technology coproduction vinyl acetate's device Download PDFInfo
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- CN205076817U CN205076817U CN201520738609.9U CN201520738609U CN205076817U CN 205076817 U CN205076817 U CN 205076817U CN 201520738609 U CN201520738609 U CN 201520738609U CN 205076817 U CN205076817 U CN 205076817U
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Abstract
The utility model discloses a heat accumulation formula carbide production technology coproduction vinyl acetate's device, including heat accumulation formula carbide production unit, heat accumulation formula carbide production unit's carbide export and the unit connection of carbide dry process acetylene, carbide dry process acetylene unit is equipped with the fresh water (FW) import, the acetylene export and the synthetic vinyl acetate unit connection of fixed bed of carbide dry process acetylene unit, the synthetic vinyl acetate unit of fixed bed is equipped with the vinyl acetate export, heat accumulation formula carbide production unit is equipped with raw coal inlet and quick lime import, the carbon monoxide unit connection is proposed with pressure swing adsorption to heat accumulation formula carbide production unit's carbide stove tail gas export, pressure swing adsorption proposes the CO export and the synthetic acetic acid unit connection of carbonylation of carbon monoxide unit, the acetic acid export and the synthetic vinyl acetate unit connection of fixed bed of the synthetic acetic acid unit of carbonylation. Have characteristics such as raw materials adaptability is wide, carbide production power consumption is few, the pollution is low, high, the economic nature of energy conversion efficiency is good.
Description
Technical field
The utility model relates to a kind of calcium carbide, acetylene, pressure-variable adsorption put forward CO, acetic acid and vinyl acetate production technology, particularly relates to a kind of device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene.
Background technology
Calcium carbide is a kind of important industrial chemicals, and usual calcium carbide is produced and referred to and blue charcoal or coke heats with lime under isolated air and hot conditions, high temperature reduction reaction occurs, finally the course of processing of acquisition finished product calcium carbide.At present, domestic existing calcium carbide production technique needs to consume the blue charcoal of a large amount of electric energy and high-quality or coke in process of production, and in air, discharge the pollutent such as large quantity of exhaust gas, dust simultaneously, the problem such as high power consumption, high pollution, high cost of current calcium carbide production technique has started seriously to restrict its Sustainable development.Particular problem is as follows: (1) adaptability to raw material is poor.Require higher to raw material granularity, the block stock of 5 ~ 30mm must be used; (2) raw materials cost is high.Must use fixed carbon higher than 82% the blue charcoal of quality block or coke; (3) production energy consumption is high.Block carbon raw and lime, mass transfer and heat transfer efficiency low, speed of reaction is lower, simultaneously, it is independently that the productive unit of the blue charcoal of raw material and calcium carbide smelt unit, cause the sensible heat of high temperature (500 ~ 800 DEG C) blue charcoal to be wasted, calcium carbide in-furnace temperature need reach more than 2200 DEG C, ton calcium carbide more than power consumption 3150kwh; (4) seriously polluted.Produce a large amount of dust pollutions in production process, energy consumption and waste water and waste gas in quenching treating processes, can be produced again.
Furnace of calcium carbide can produce a large amount of tail gas in process of production, containing the carbon monoxide of about 80% in tail gas, also containing a large amount of dust and a small amount of hydrogen, carbonic acid gas, nitrogen, methane, oxygen, also have sulfide, phosphide, carbide, calcium and magnesium oxides, coal tar wet goods tens kinds of compositions in addition.Under normal circumstances, after being through dust removal process, directly discharging or be used as fuel, along with the maturation of wet dedusting technology, the integral utilization space of calcium carbide stove exhaust is also increasing, but to be separated CO, CH wherein further
4, H
2etc. component, make it become the unstripped gas can producing the Chemicals such as synthetic ammonia and methyl alcohol, not only investment is large, and running cost is high, and alternative mature technology is also little.
Existing calcium carbide production technology remains to be further improved, and the comprehensive utilization of calcium carbide stove exhaust also needs to be researched and developed further.The device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene has no report.
Utility model content
The purpose of this utility model is to provide the device of a kind of energy-saving and environmental protection, heat accumulating type calcium carbide production technique coproduction by acetic acid ethene that efficiency is high.
The purpose of this utility model is achieved through the following technical solutions:
The device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene of the present utility model, comprise heat accumulating type calcium carbide productive unit, the calcium carbide outlet of described heat accumulating type calcium carbide productive unit is connected with calcium carbide drying acetylene unit, the acetylene outlet of described calcium carbide drying acetylene unit is connected with fixed bed synthesizing vinyl acetate unit, described fixed bed synthesizing vinyl acetate unit is provided with vinyl acetate between to for plastic outlet, described heat accumulating type calcium carbide productive unit is provided with raw coal inlet and unslaked lime import, the calcium carbide stove exhaust outlet of described heat accumulating type calcium carbide productive unit is carried carbon monoxide unit with pressure-variable adsorption and is connected, the CO outlet that described pressure-variable adsorption carries carbon monoxide unit is connected with carbonylation acetic acid unit, the acetic acid outlet of described carbonylation acetic acid unit is connected with described fixed bed synthesizing vinyl acetate unit, described calcium carbide drying acetylene unit is provided with process water import, described carbonylation acetic acid unit is connected with methyl alcohol import.
The technical scheme provided as can be seen from above-mentioned the utility model, the device of the heat accumulating type calcium carbide production technique coproduction by acetic acid ethene that the utility model embodiment provides, coal pyrolysis and calcium carbide are produced and is coupled, be integrated with heat storage type combustion, radiator tube heating, rotating bed high temperature pyrolysis, high-temperature hot send the modern techniquies such as material to, subversive use powdery raw coal and unslaked lime prepare calcium carbide for raw materials for production.Compared with traditional calcium carbide production technique, there is the features such as adaptability to raw material is wide, calcium carbide production power consumption is few, it is low to pollute, energy conversion efficiency is high, good economy performance.Simultaneously, recycled by calcium carbide stove exhaust, adopt pressure-swing absorption apparatus, extract the CO in calcium carbide stove exhaust, with acetic acid synthesis from methanol carbonylation, the acetylene reaction that acetic acid obtains with dry method calcium carbide again generates vinyl acetate between to for plastic, forms long and complete industrial chain, recycling economy feature is obvious, and product comprehensive competitive power is strong.
Accompanying drawing explanation
The structural representation of the device of the heat accumulating type calcium carbide production technique coproduction by acetic acid ethene that Fig. 1 provides for the utility model embodiment.
In figure: 1-heat accumulating type calcium carbide productive unit; 2-calcium carbide drying acetylene unit; 3-pressure-variable adsorption carries carbon monoxide unit; 4-carbonylation acetic acid unit; 5-fixed bed synthesizing vinyl acetate unit.
Embodiment
To be described in further detail the utility model embodiment below.
The device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene of the present utility model, its preferably embodiment be:
Comprise heat accumulating type calcium carbide productive unit, the calcium carbide outlet of described heat accumulating type calcium carbide productive unit is connected with calcium carbide drying acetylene unit, the acetylene outlet of described calcium carbide drying acetylene unit is connected with fixed bed synthesizing vinyl acetate unit, described fixed bed synthesizing vinyl acetate unit is provided with vinyl acetate between to for plastic outlet, described heat accumulating type calcium carbide productive unit is provided with raw coal inlet and unslaked lime import, the calcium carbide stove exhaust outlet of described heat accumulating type calcium carbide productive unit is carried carbon monoxide unit with pressure-variable adsorption and is connected, the CO outlet that described pressure-variable adsorption carries carbon monoxide unit is connected with carbonylation acetic acid unit, the acetic acid outlet of described carbonylation acetic acid unit is connected with described fixed bed synthesizing vinyl acetate unit, described calcium carbide drying acetylene unit is provided with process water import, described carbonylation acetic acid unit is connected with methyl alcohol import.
Described heat accumulating type calcium carbide productive unit comprises material processing device, rotating bed dry distillation of coal device, furnace of calcium carbide device and dry distillation gas refining plant.
Described calcium carbide drying acetylene unit comprises acetylene generator and acetylene cleaning device.
Described pressure-variable adsorption is carried carbon monoxide unit and is comprised calcium carbide stove exhaust pretreatment unit, compression set, de-aerator plant and pressure-swing absorption apparatus.
Described carbonylation acetic acid unit comprises acetic acid reaction device and acetic acid refining device.
Described fixed bed synthesizing vinyl acetate unit comprises vinyl acetate synthesis device, vinyl acetate between to for plastic rectifier unit and exhaust recovery device.
The device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene of the present utility model, overcome the defect of traditional calcium carbide production technology, creationary coal pyrolysis and calcium carbide productions of this device is coupled, be integrated with heat storage type combustion, radiator tube heating, rotating bed high temperature pyrolysis, high-temperature hot send the modern techniquies such as material to, subversive use powdery raw coal and unslaked lime prepare calcium carbide for raw materials for production.Compared with traditional calcium carbide production technique, there is the features such as adaptability to raw material is wide, calcium carbide production power consumption is few, it is low to pollute, energy conversion efficiency is high, good economy performance.Simultaneously, recycled by calcium carbide stove exhaust, adopt pressure-swing absorption apparatus, extract the CO in calcium carbide stove exhaust, with acetic acid synthesis from methanol carbonylation, the acetylene reaction that acetic acid obtains with dry method calcium carbide again generates vinyl acetate between to for plastic, forms long and complete industrial chain, recycling economy feature is obvious, and product comprehensive competitive power is strong.
The device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene, the by product produced in calcium carbide production process is fully utilized, also " newly-built calcium carbide production equipment must enter industrial park, and has corresponding downstream industry supporting with it " requirement is met in " calcium carbide industry entry criteria (2014 revision) ".
Specific embodiment:
As shown in Figure 1, comprise as lower unit: heat accumulating type calcium carbide productive unit 1, calcium carbide drying acetylene unit 2, pressure-variable adsorption carry carbon monoxide unit 3, carbonylation acetic acid unit 4, fixed bed synthesizing vinyl acetate unit 5.Wherein:
Described heat accumulating type calcium carbide productive unit 1, comprises Feedstock treating operation, rotating bed dry distillation of coal operation, furnace of calcium carbide operation, dry distillation gas cleaning section;
Described Feedstock treating operation is the treatment system of raw material, and major function is feed coal, the reception of unslaked lime and feed coal, the fragmentation of unslaked lime, ore grinding, batching, mixing, agglomeration, with the qualified agglomeration of the requirement meeting pyrolysis rotating bed;
Described rotating bed dry distillation of coal operation, the shaping pelletizing of agglomeration that Feedstock treating operation is come, through retort process, generation oil gas and active pelletizing deliver to downstream calcium carbide furnaceman sequence process, and technological process is: oil gas-hot discharging of remaining solid thing is discharged in charging-heat temperature raising pyrolysis-pyrolysis;
Described furnace of calcium carbide operation, solids--the active pelletizing that process rotating bed dry distillation of coal operation produces, produces calcium carbide product, simultaneously by-product calcium carbide stove exhaust;
Described dry distillation gas cleaning section obtains tar, crude benzol and clean coal gas by obtaining oil gas after dry distillation of coal pyrolysis through refrigerated separation;
Described calcium carbide drying acetylene unit 2, comprises acetylene generation operation and acetylene cleaning operation;
Described acetylene generation operation, reacts in device at acetylene, and water to be sprayed on water smoke state through nozzle and calcium carbide to make it hydrolysis and generate thick acetylene gas;
Described acetylene cleaning operation, after thick acetylene gas is lowered the temperature by cooling tower, enters peace and quiet tower, adopts sulphate method to carry out peace and quiet, finally enters washing tower removing acidic substance, obtains smart acetylene gas;
Described pressure-variable adsorption carries carbon monoxide unit 3, comprises calcium carbide stove exhaust pre-treatment, compression, deoxygenation and pressure-variable adsorption operation;
Described pressure-variable adsorption operation is by CO and H
2, CH
4, N
2be separated Deng other impurity component, obtain CO gas product, adopt multiple adsorption tower alternation flow process, in one cycle, adsorption tower experiences successively: absorption, drop pressure, displacement, reversely to bleed off pressure, vacuumize, boost pressure, preadsorption, the technological process such as whole pressurising, isolate pure CO;
Described carbonylation acetic acid unit 4, comprises acetic acid reaction operation and acetic acid refining operation;
Described acetic acid reaction operation, refers to that material benzenemethanol and carbon monoxide pass into reactor by a certain percentage continuously, carries out reaction and generate thick acetic acid under catalyst action;
Described acetic acid refining operation, is made up of lightness-removing column, dehydration tower, finishing column and spent acid stripping tower, output acetate products;
Described fixed bed synthesizing vinyl acetate unit 5, comprises vinyl acetate synthesis operation, vinyl acetate between to for plastic rectification working process and exhaust gas recovery operation;
Described vinyl acetate synthesis operation, the acetylene gas adopting calcium carbide to produce and acetic acid carry out building-up reactions and generate thick vinyl acetate between to for plastic in calandria type fixed bed reactor;
Described vinyl acetate between to for plastic rectification working process, is made up of degassing tower, primary tower, extraction tower and rectifying tower, output vinyl acetate between to for plastic product;
Described exhaust gas recovery operation, the component loops gas that process vinyl acetate synthesis operation is discharged, and the acetylene gas that degassed tower top is discharged, reclaim by acetic acid washing tower, soda-wash tower, pickling tower the acetic acid containing acetylene, deliver to vinyl acetate synthesis operation and recycle.
The utility model has following technical characterstic and beneficial effect:
1. heat accumulating type calcium carbide production technique
(1) creatively coal pyrolysis technique and calcium carbide production technique are coupled.Adaptability to raw material is wide, cheap, does not need the high-quality resources such as coke, semicoke, hard coal as raw material in production process, and only need use cheap middle low order, powdery coal resources, ton carbide raw material cost reduces by more than 300 yuan;
(2) process energy consumption is low, thermo-efficiency is high.Adopt regenerative combustion technology, radiator tube heating technique, rotating bed high temperature pyrolysis technology, high-temperature hot to send fed technology, take full advantage of the sensible heat of product in calcium carbide production process, integrated artistic thermo-efficiency is high, and calcium carbide per ton reduces technique power consumption more than 300 degree;
(3) environmental friendliness.This technique achieves the complete utilization of powder raw material, solves the problem that in calcium carbide production process, dust pollution is serious from source.Simultaneously raw coal with lime pelletizing by pyrolysis processing time, can remove the harmful element such as sulphur and mercury in coal in a large number, in production process, the quantity discharged of the atmospheric polluting material such as oxynitride, oxysulfide, PM2.5 is than traditional technology decline more than 80%;
(4) good economy performance.Adopt powder coal as raw material at a low price, the tar that in pyrolytic process, energy by-product is a large amount of and coke-oven gas, greatly improve the economy of integrated artistic, and ton calcium carbide income improves 500 ~ 800 yuan;
2. calcium carbide dry acetylene generation process
(1) water consumption is few, safety.Calcium carbide continuous charging process, and in about 95 DEG C drying acetylene technique gas phases, water vapour content is higher, improves the safety and stability of reaction generation systems; In addition, during malfunction, because calcium carbide in dry acetylene generation process producer and micro-excessive water react, the reaction of calcium carbide and water can stop fast;
(2) carbide slag applying unit energy consumption is reduced.The carbide slag water content that dry acetylene generation process produces, generally below 10%, directly as the raw material producing cement, can reduce the fragmentation of manufacture of cement Raw, oven dry etc. and produces load;
(3) consumption of calcium carbide is low.Dry acetylene generation process, owing to adopting continuous enter material way, avoids by the reinforced acetylene emptying loss caused of bucket, improves the yield of acetylene, decrease the consumption of calcium carbide, reduce production cost;
3. pressure-variable adsorption puies forward carbon monoxide technique, adopts high efficiency carbon monoxide adsorbent, multiple adsorption tower alternation thus reach the object being continuously separated purification CO, and technical process is advanced, unstripped gas adaptability is good, level of automation is high;
4. carbonylation acetic acid technology, reaction conditions is gentle, and catalyst performance stabilised, activity is high, selectivity good; Product yield is high, and quality is good and without byproduct; Technological process is simple, stable operation, safe and reliable, keep in repair easy; The three wastes are few pollution-free; Starting material and power consumption low, good in economic efficiency;
5. fixed bed synthesizing vinyl acetate technique
(1) fixed bed bed pressure drop is low.Lower to the requirement of reactor inlet pressure, about inlet pressure 0.04MPaG just can meet the requirement of building-up reactions;
(2) catalyst activity is high.Adopt the gac being different from fluidized-bed to be support of the catalyst, add its distinctive collocation method, good catalyst activity, the life-span is long;
(3) catalyzer space-time yield is high.The reaction raw materials mol ratio of fixed-bed process is far away higher than fluidized-bed process, and in bed, acetylene dividing potential drop is high, and speed of reaction is fast, and thus the catalyzer of unit volume has higher space-time yield;
(4) synthesis unit has energy-conservation advantage.The energy-conservation of synthesis unit is mainly reflected in acetic acid evaporative process and vapour gas heat transfer process, and fixed-bed process acetic acid per pass conversion can reach 75%, far away higher than the per pass conversion of fluidized-bed process 25-40%;
6. utilize low order fine coal, unslaked lime and methyl alcohol for raw material, carbon monoxide unit, carbonylation acetic acid unit and fixed bed synthesizing vinyl acetate unit combination technique is put forward by heat accumulating type calcium carbide productive unit, calcium carbide drying acetylene unit, pressure-variable adsorption, calcium carbide, acetylene, acetic acid, vinyl acetate between to for plastic can be produced, form long and complete industrial chain, recycling economy feature is obvious, and product comprehensive competitive power is strong.A whole set of combination process has less investment, fecund, efficient, production process is simple, can quantity-produced remarkable advantage.
7. from calcium carbide furnace gas, extract carbon monoxide and then for the preparation of acetic acid, turn waste into wealth, environmental friendliness, production cost is low, economic benefits.
8. the utility model is while production calcium carbide, vinyl acetate between to for plastic, and the high value added products such as by-product coal tar, crude benzol, sulphur, sulphur ammonium, acetaldehyde, make whole set process more economically, have more wide industrial prospect.
9. pass through techno-economical accounting, adopting the combination preparing device financial internal rate of return of this whole set process after-tax is 22.57%, profitability can meet industry requirement, show from the every performance indicator of combination preparing device, the break even etc., adopt the combination preparing device of this whole set process to have the good ability to ward off risks.
The principle of work of specific embodiment is:
As shown in Figure 1, mainly comprise heat accumulating type calcium carbide productive unit 1, calcium carbide drying acetylene unit 2, pressure-variable adsorption carry carbon monoxide unit 3, carbonylation acetic acid unit 4, fixed bed synthesizing vinyl acetate unit 5, be connected successively by pipeline.Device described in the utility model with low order powdery raw coal and unslaked lime for raw material, by heat accumulating type calcium carbide production technique output calcium carbide, dry method obtains acetylene gas again, after calcium carbide stove exhaust delivers to pressure-swing absorber extraction carbon monoxide, with acetic acid synthesis from methanol carbonylation, acetic acid again with acetylene in fixed-bed reactor synthesizing vinyl acetate.
1. heat accumulating type calcium carbide productive unit
Calcium carbide for raw material, adopts heat accumulating type calcium carbide production technique with feed coal, unslaked lime, i.e. raw materials pretreatment+agglomeration+rotating bed destructive distillation+active pelletizing heat send+furnace of calcium carbide smelting technology production calcium carbide.
Feed coal, unslaked lime and binding agent (molasses and aluminium dihydrogen phosphate) are broken respectively, be milled to granularity and send into proportioning room for after-100 orders, the intensive mixer sending into mixing moulding room after preparing burden according to 1:1.3 ~ 1.6:0.1 ~ 0.3 ratio mixes, qualified blend feedstock is provided to surge bunker after mixing machine mixing material, mixing raw material in surge bunker enters spiral heating transfer roller by screw feeder dosing, spiral heating transfer roller sends behind mixed material heating to 80 ~ 120 DEG C into forming machine, the mixing raw material that blend feedstock is shaped to 30mm × 25mm × 13mm by forming machine is sent to rotating bed.
What transport from raw material preparation system sieves through pressure ball many lattice feed bin that qualified raw material enters rotating bed pyrolysis oven charging bole top, the feeding machine device of feed opening is unloaded by being located at every lattice feed bin, feed in stove, automatically control the flow of expecting according to furnace bottom velocity of rotation, meet the requirement of continuous cloth.Lump coal is thick at rotating bed upper berth 100 ~ 200mm.
The furnace bottom uniform rotation of rotating bed pyrolysis oven, carries the cleaned coal of cloth on furnace bottom and passes through each section successively.By velocity of rotation at the bottom of regulating stove, material block can be changed and heat up in stove time of pyrolysis.The intensification pyrolysis time of material block in stove is generally 1 ~ 2 hour.
Rotating bed pyrolysis installation circular ring type burner hearth is divided into loading area, preheating one district, preheating two district, reacts a district to reaction totally eight control regions and discharge zone, 6th district.Pyrolysis compound moves with rotating bed, pyrolytic process is completed after experiencing above-mentioned each district, releasing oil gas is sent to oil gas collection district and carries out gas-oil separation, remaining temperature is that about 650 DEG C hot pelletizings are transported to furnace of calcium carbide feed bin by high-temperature material movement system, then to be sent in stove by raw material by filling tube via calcium carbide furnace charging device and smelt.
Be contained in the qualified electrode paste in electrode lifting bucket, rise to electrode shell top through overhead [rope from ground and pour in electrode container.
Electric energy inputs in stove by transformer and conducting system through self baking electrode;
The sensible heat that pyrolysis feed pelletizing is taken out of by arc heat, resistance heat, carbon monoxide, is heated to 1700 ~ 2000 DEG C, generates calcium carbide, by-product calcium carbide stove exhaust.
The calcium carbide smelted, comes out of the stove once every a hours from fire door, and melting calcium carbide flows in the calcium carbide pot on trailer wagon, moves dolly to cooling factory building cool by windlass.
The raw gas (500 ~ 700 DEG C) come by rotating bed pyrolysis oven goes out profit and raw gas (~ 85 DEG C) with after cyclic ammonia water Quench by gas-liquid separator separates.Wherein profit enters water-and-oil separator and isolates tar and recirculated water, and a recirculated water part enters ammonia steaming device and reclaims ammonia, a part of circulation Quench; Raw gas enters cooling tower and is cooled to 22 DEG C further, by electrical tar precipitator, gas blower send into thiamine recovery device reclaim sulphur ammonium after (55 DEG C) enter cooling tower and be cooled to 26 DEG C, then wash after benzene (30 DEG C) enters thionizer desulfurization obtain clean coal gas by washing benzene tower; Sulfur removing pregnant solution regenerates after entering reactive tank, regenerator column, and the foam floating on tower top enters sulfur melting kettle heating and melting and produces sulphur.
2. calcium carbide drying acetylene unit
Calcium carbide ensures that after fragmentation particle diameter is less than 3 millimeters, adds producer hermetically continuously by the metering screw handling machinery with tightness system.The water being slightly more than theoretical amount enters carbide-feed generator by the interface on producer, to be sprayed on mist state by nozzle and calcium carbide to make it hydrolysis, temperature of reaction gas phase is 90 ~ 100 DEG C, solid-state temperature is 100 ~ 110 DEG C, reaction heat is taken away by water vapor, passes to recirculated water (not having solution loss) via contactless interchanger.6 layers of column plate are had in producer, all there is stirring, every layer of residence time of material about 1 ~ 2 minute, material completes about 13 ~ 14 minutes from entering reaction, the acetylene gas that reaction generates is discharged from top, carbide slag is from reactor bottom by spiral squeezing, and the carbide slag of generation is the dry powder of water content 5% ~ 10%.Feed in raw material and slag tap and all adopt nitrogen gas seal equipment.
First enter cooling one tower from producer thick acetylene gas out and carry out cooling washing, after water ring compressor supercharging, enter cooling two tower again carry out cooling and dewater, the thick acetylene gas with a small amount of steam come by cooling tower, after boosting, enter the first peace and quiet tower successively, the second peace and quiet tower purifies, in peace and quiet tower, adopt sulphate method to carry out peace and quiet, finally enter washing tower removing acidic substance, fixed bed synthesizing vinyl acetate unit delivered to by the smart acetylene gas after peace and quiet.
3. pressure-variable adsorption carries carbon monoxide unit
In one cycle, adsorption tower experiences successively: absorption, drop pressure, displacement, reversely to bleed off pressure, vacuumize, boost pressure, preadsorption, the technological process such as whole pressurising.
Calcium carbide stove exhaust after deoxygenation is sent in the adsorption tower of pressure-variable adsorption operation, and under predetermined adsorptive pressure, the CO in gas mixture is absorbed by Special adsorbent, H
2, CH
4, N
2deng not flowed out from absorption tower top as absorption tail gas by the component that adsorbs.After the forward position, CO mass transfer zone in adsorption tower arrives the predetermined position of adsorption tower, close imported valve and the absorption tail gas outlet valve of adsorption tower unstripped gas, adsorption tower stops adsorption step, starts to proceed to regenerative process.
After terminating adsorption step, adsorption tower is communicated with the adsorption tower being in low pressure successively, the useful component in adsorption tower dead-space volume is reclaimed.
After drop pressure terminates, at the bottom of adsorption tower, import adsorption tower along absorption direction with part CO gas product, impurity component remaining in adsorption tower is forward replaced away, thus makes the CO in adsorption tower meet the requirements of purity.Because the CO content in displacement tail gas is very high, in order to reclaim this part gas, by being first in the adsorption tower of boost process before displacement tail gas outflow system by one, a part of CO can be reclaimed like this, i.e. preadsorption step.
Through above a series of operation steps, the CO purity in adsorption tower has reached product specification requirement, and now to open bottom adsorption tower reverse bleeds off pressure valve, and against absorption direction, adsorption column pressure is down to normal pressure, inverse put gas enters inverse put gas surge tank.
Reverse bleed off pressure end after, with vacuum pump against absorption direction adsorption tower is vacuumized, make to be able to desorb up hill and dale by the CO adsorbed, the CO that desorb is got off enters gas product surge tank.
From the displacement tail gas of other tower, enter this adsorption tower and carry out preadsorption with recovery part CO, reduce the loss of CO.
After preadsorption step completes, successively boost pressure is carried out to this adsorption tower with the elevated pressures gas from other adsorption tower, the pressure of adsorption tower is raised gradually, final equal with the pressure of the adsorption tower be interconnected.
The pressure that experienced by the adsorption tower of each boost pressure step above does not also reach predetermined adsorptive pressure, can be switched to reposefully to make the material in adsorption tower and adsorb next time, by the absorption tail gas of the adsorption tower being in adsorption step, the pressure of adsorption tower be risen to predetermined adsorptive pressure.
So far, adsorption tower completes a complete adsorption-regeneration cycles process, and gets ready for next working cycle.
4. carbonylation acetic acid unit
Pass into reactor continuously by a certain percentage through the material benzenemethanol of preheating and carbon monoxide, react under catalyst action.During driving, reaction solution driving pump delivery circulates to driving well heater, the tail gas that during normal running, reaction solution and reactor discharge enters conversion reactor continuously and carries out second time reaction, the catalyzer complex compound of instability is converted into stable catalyst complex, and then gas phase goes Light ends recovery system; Liquid phase sends into flash drum, carries out gas-liquid separation, and isolate liquid containing catalyzer by catalyst recirculation pumped back reactor, flash drum top expellant gas contains the materials such as acetic acid, delivers to acetic acid refining system.
Acetic acid refining system is made up of cut light tower, dehydration tower, finishing column and spent acid stripping tower, the gaseous phase materials come from synthesis procedure is introduced into cut light tower, top gaseous phase is through condensation layering, part light liquid returns stream mutually, all the other whole Returning reactors, the liquid returning reactor of discharging at the bottom of tower, thick acetic acid, from the lateral line discharging of lightness-removing column, enters dehydration tower.
The moisture gas phase of dehydration tower top is through condensation, and partial reflux, all the other recycled back reactors, the Glacial acetic acid obtained at the bottom of tower enters finishing column and distills, and at the bottom of this tower, discharge a small amount of heavy constituent that reaction generates, product acetic acid, from this tower side take-off, delivers to acetic acid basin.From a small amount of light constituent that finished product tower top is discharged, through condenser condenses, partial reflux, all the other circulations turn back to dehydration tower.
The acetic acid containing heavy constituent of discharging at the bottom of finishing column enters spent acid stripping tower and carries out stripping, and top gaseous phase returns finishing column, and the waste liquid of discharging containing propionic acid at the bottom of tower sends to burning.
Light constituent recovery system is made up of high and low pressure absorption tower.The emission gases carrying out autoreactor enters high-pressure absorber, with the methyl iodide in methanol absorption emission gases, the gas of acetic acid refining system enters low-pressure absorption tower and also uses methyl iodide in methanol absorption emission gases, the materials at bottom of tower on high-low pressure absorption tower is as the methanol feeding of reactor, emission gases, main component is CO, CO
2and H
2deliver to torch.
5. fixed bed synthesizing vinyl acetate unit
Raw material acetic acid enters acetate evaporator, it is overheated that acetic acid steam after evaporation enters acetic acid superheater again, then mix with through gas/oil interchanger acetylene gas out laggard enter calandria type fixed bed reactor, the mixture of acetic acid steam and excessive acetylene flows through the impregnated activated-carbon catalyst of zinc acetate in reactor under the pressure of 0.03 ~ 0.05MPaG, react at 160 ~ 210 DEG C, generate thick vinyl acetate between to for plastic.The thermal oil that reaction liberated heat is recycled is withdrawn, and temperature of reaction is controlled by Reactor inlet oil temperature.
Gas mixture after building-up reactions enters condensing tower, and condensed liquid is sent to vinyl acetate between to for plastic rectification working process, is made up of degassing tower, primary tower, extraction tower and rectifying tower, output vinyl acetate between to for plastic product; The component loops gas that vinyl acetate synthesis operation is discharged, and the acetylene gas that degassed tower top is discharged, deliver to exhaust gas recovery operation, reclaims the acetic acid containing acetylene, deliver to vinyl acetate synthesis operation and recycle by acetic acid washing tower, soda-wash tower, pickling tower.
The above; be only the utility model preferably embodiment; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; the change that can expect easily or replacement, all should be encompassed within protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims.
Claims (6)
1. the device of a heat accumulating type calcium carbide production technique coproduction by acetic acid ethene, it is characterized in that, comprise heat accumulating type calcium carbide productive unit, the calcium carbide outlet of described heat accumulating type calcium carbide productive unit is connected with calcium carbide drying acetylene unit, the acetylene outlet of described calcium carbide drying acetylene unit is connected with fixed bed synthesizing vinyl acetate unit, described fixed bed synthesizing vinyl acetate unit is provided with vinyl acetate between to for plastic outlet, described heat accumulating type calcium carbide productive unit is provided with raw coal inlet and unslaked lime import, the calcium carbide stove exhaust outlet of described heat accumulating type calcium carbide productive unit is carried carbon monoxide unit with pressure-variable adsorption and is connected, the CO outlet that described pressure-variable adsorption carries carbon monoxide unit is connected with carbonylation acetic acid unit, the acetic acid outlet of described carbonylation acetic acid unit is connected with described fixed bed synthesizing vinyl acetate unit, described calcium carbide drying acetylene unit is provided with water smoke import, described carbonylation acetic acid unit is connected with methyl alcohol import.
2. the device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene according to claim 1, it is characterized in that, described heat accumulating type calcium carbide productive unit comprises material processing device, rotating bed dry distillation of coal device, furnace of calcium carbide device and dry distillation gas refining plant.
3. the device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene according to claim 1, it is characterized in that, described calcium carbide drying acetylene unit comprises acetylene generator and acetylene cleaning device.
4. the device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene according to claim 1, it is characterized in that, described pressure-variable adsorption is carried carbon monoxide unit and is comprised calcium carbide stove exhaust pretreatment unit, compression set, de-aerator plant and pressure-swing absorption apparatus.
5. the device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene according to claim 1, it is characterized in that, described carbonylation acetic acid unit comprises acetic acid reaction device and acetic acid refining device.
6. the device of heat accumulating type calcium carbide production technique coproduction by acetic acid ethene according to claim 1, it is characterized in that, described fixed bed synthesizing vinyl acetate unit comprises vinyl acetate synthesis device, vinyl acetate between to for plastic rectifier unit and exhaust recovery device.
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| CN201520738609.9U CN205076817U (en) | 2015-09-22 | 2015-09-22 | Heat accumulation formula carbide production technology coproduction vinyl acetate's device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174262A (en) * | 2015-09-22 | 2015-12-23 | 北京华福工程有限公司 | Vinyl acetate production device and method in cooperation with heat accumulating type calcium carbide production process |
| CN106125690A (en) * | 2016-08-04 | 2016-11-16 | 石河子开发区天业化工有限责任公司 | Acetylene production process operation displacement and the control method fed |
-
2015
- 2015-09-22 CN CN201520738609.9U patent/CN205076817U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174262A (en) * | 2015-09-22 | 2015-12-23 | 北京华福工程有限公司 | Vinyl acetate production device and method in cooperation with heat accumulating type calcium carbide production process |
| CN105174262B (en) * | 2015-09-22 | 2018-01-30 | 北京华福工程有限公司 | The apparatus and method of heat accumulating type calcium carbide production technology coproduction by acetic acid ethene |
| CN106125690A (en) * | 2016-08-04 | 2016-11-16 | 石河子开发区天业化工有限责任公司 | Acetylene production process operation displacement and the control method fed |
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