CN201305565Y - Device for preparing formaldehyde by exhaust gas circulation process - Google Patents
Device for preparing formaldehyde by exhaust gas circulation process Download PDFInfo
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- CN201305565Y CN201305565Y CNU2008201599655U CN200820159965U CN201305565Y CN 201305565 Y CN201305565 Y CN 201305565Y CN U2008201599655 U CNU2008201599655 U CN U2008201599655U CN 200820159965 U CN200820159965 U CN 200820159965U CN 201305565 Y CN201305565 Y CN 201305565Y
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Abstract
The utility model relates to a device for preparing formaldehyde by exhaust gas circulation process, and the device comprises a methanol pump (1), a methanol filter (2), an air filter (3), an exhaust gas blower (4), a methanol reboiler (5), a Roots blower (6), an exhaust gas heater (7), a methanol evaporator (8), an air heater (9), a quaternary gas mixer (10), a steam filter (11), a steam distributor (12), a quaternary gas filter (13), a fixed-bed type oxidizer (14), a first absorption tower (15), an intermediate trap (16), a first tower plate heat exchanger (17), a first tower circulating pump (18), a second absorption tower (19), a terminal trap (20), a second tower plate heat exchanger II (21), a second tower circulating pump II (22), a second tower circulating pump I (23), a second tower plate heat exchanger I (24), an exhaust gas liquid seal trough (25) and an exhaust gas processor (26). The device has the advantages of reasonable energy utilization, stable production, low unit consumption of methanol and adjustable concentration of formaldehyde.
Description
(1) technical field
The utility model relates to a kind of exhaust gas circulation process that is used to produce 37%～55% formaldehyde solution and produces formaldehyde plant.
(2) background technology
At present, the method that realizes suitability for industrialized production formaldehyde solution both at home and abroad mainly contains the different technology of two classes.The first adopts " the methyl alcohol overflow method " of silver catalyst, also claims silver-colored catalysis method.It two is " the air excess methods " that adopt the iron-molybdenum oxide catalyzer, also claims iron molybdenum catalysis method.Conventional silver catalysis method advantage is that investment is little, power consumption is low, and shortcoming is a methyl alcohol unit consumption height, methanol content height in the formaldehyde, concentration of formaldehyde low (about 37%).The advantage of iron molybdenum catalysis method is that the methyl alcohol unit consumption is low, and methanol content is low in the formaldehyde, the concentration of formaldehyde height, and shortcoming is that acid number is higher, investment is big, power consumption is high.
Traditional silver-colored catalysis method is produced formaldehyde technical process (Fig. 2), and to be methyl alcohol go into vaporizer through filter is laggard, control certain liquid level and vaporization temperature, air by the Root's blower air blast enter the vaporizer bubbling by methyl alcohol and with its vapor mixing, allocate a certain amount of water vapor at the evaporator outlet place again, form methyl alcohol-air-water vapor three-element mixed gas body.This three-element mixed gas body is superheated to 100～140 ℃ and removes detrimental impurity such as iron carbonyl after filtration and enter oxidation reactor, and methyl alcohol generates formaldehyde through peroxidation, dehydrogenation reaction under the effect of silver catalyst.Reaction product quenching immediately (reaction heat is used to produce steam) further is cooled to 80～90 ℃ indirectly again and enters absorption system to 230 ℃.Absorption system is made up of two absorption towers, first absorption tower very useful second absorbs the rare formalin spray at the bottom of the Tata, formaldehyde gas its product after absorbing is discharged at the bottom of absorbing Tata by first, and unabsorbed formaldehyde and other gases are discharged from the first absorption tower cat head and entered second absorption tower.Two column overhead absorb once more with the process water spray, and rare formalin partly refluxes.The tail gas that goes out two cats head is sent into the tail gas boiler and is made fuel and use.The traditional technology catalyzer generally adopts outward appearance to be the spongiform sponge silver of macrofiber, the sponge silver main drawback be work-ing life short, poison resistance is poor, the device cycle of operation was generally 1～2 month.
(3) summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency, a kind of reasonable energy utilization is provided, produces the exhaust gas circulation process stable, that the methyl alcohol unit consumption is low, concentration of formaldehyde is adjustable (37%～55%) and produce formaldehyde plant.
The purpose of this utility model is achieved in that a kind of exhaust gas circulation process produces formaldehyde plant, it is characterized in that described device comprises methanol pump, the methyl alcohol strainer, air filter, the tail gas gas blower, the methyl alcohol reboiler, Root's blower, heater exhaust gas, methanol evaporator, airheater, the quaternary gas mixer, vapor filter, vapour distributor, the quaternary gas filter, the fixed-bed type oxidizer, first absorption tower, middle trap, one column plate type interchanger, one tower recycle pump, second absorption tower, the terminal trap, two column plate type interchanger II, two tower recycle pump II, two tower recycle pump I, two column plate type interchanger I, tail gas liquid seal trough and exhaust gas treating device, described methanol pump discharge port links to each other with methyl alcohol strainer opening for feed, methyl alcohol strainer discharge port links to each other with methyl alcohol reboiler bottom, methyl alcohol reboiler top links to each other with methanol evaporator is middle, the methanol evaporator top links to each other with the import of quaternary gas mixer, and the methanol evaporator bottom links to each other with the methyl alcohol reboiler; Described air filter outlet links to each other with the Root's blower import, the Root's blower outlet links to each other with the airheater import, the airheater outlet links to each other with the import of quaternary gas mixer, the vapour distributor import links to each other with fixed-bed type oxidizer vapour outlet, the vapour distributor outlet links to each other with the vapor filter import, and the vapor filter outlet links to each other with the import of quaternary gas mixer; The tail gas blower export links to each other with the heater exhaust gas import, the heater exhaust gas outlet links to each other with the import of quaternary gas mixer, the outlet of quaternary gas mixer links to each other with the import of quaternary gas filter, the outlet of quaternary gas filter links to each other with the import of fixed-bed type oxidizer, the formaldehyde gas-liquid mixture outlet of fixed-bed type oxidizer links to each other with the first absorption tower import, bottom, first absorption tower links to each other with a tower pump inlet, one tower circulating-pump outlet links to each other with a column plate type interchanger import, one column plate type heat exchanger exit divides two the tunnel, one the tunnel is connected with pipeline, another road absorbs additional liquid import with top, first absorption tower and links to each other, the first absorption tower top exit links to each other with middle trap, middle trap gaseous phase outlet links to each other with the second absorption tower import, middle trap liquid phase outlet links to each other with top, first absorption tower, bottom, second absorption tower links to each other with two tower recycle pump I imports, two tower recycle pump I outlet links to each other with two column plate type interchanger I imports, two column plate type interchanger I outlet divides two the tunnel, one the tunnel links to each other with second absorption tower middle part, another road links to each other with bottom, first absorption tower, two tower recycle pump II imports link to each other with middle part, second absorption tower, two tower recycle pump II outlet links to each other with two column plate type interchanger II imports, two column plate type interchanger II outlet replenishes the absorption liquid import with top, second absorption tower and links to each other, the tail gas outlet of top, second absorption tower links to each other with the terminal trap, the outlet of terminal trap tail gas divides two the tunnel, one the tunnel links to each other with the tail gas liquid seal trough, the tail gas liquid seal trough links to each other with exhaust gas treating device, and another road links to each other with the tail gas blower inlet.
The utility model is with (or the part waste gas behind the exhaust combustion of the part tail gas in the formaldehyde production, also claim stack gas) substitute in the traditional technology partly or all water vapor as the thermo-stabilizer of reaction heat, form quaternary or three-element mixed gas with methyl alcohol and air, the demand that can recently realize producing the formaldehyde (37%～55%) of different concns with low water alcohol in process of production.The water alcohol of traditional technology production requirement elects 1～1.4 as than generally, it sets out for the security standpoint of control reaction temperature, but also limited its product concentration and can not do height, and thereby the utility model has substituted portion water steam has reduced water alcohol ratio as thermo-stabilizer requirement because of tail gas, Here it is, and the utility model can be done the key point of high-concentration formaldehyde, and the utility model is generally selected water alcohol for use than being 0.8～0.9.
The utility model has overcome the binary gas or the ternary gas methodology of traditional technology and can not accurately control the shortcoming of oxygen-methanol ratio, water alcohol ratio and adopt quaternary gas-operated method, be that methyl alcohol is squeezed into methyl alcohol reboiler, methanol evaporator by methanol pump, behind heating evaporation, methanol gas enters the quaternary gas mixer; Air is sent into airheater by Root's blower, enters the quaternary gas mixer after preheating; The suitable earlier batching water vapor that adds enters the quaternary gas mixer, and after production was normal, exhaust system purged displacement with tail gas, opens to enter the quaternary gas mixer after the tail gas gas blower makes part tail gas by the heater exhaust gas preheating again.Four kinds of gas with various have all separately that the autonomous channel independent control adds respectively, can accurately control oxygen-methanol ratio, water alcohol by metrical instrument like this and processing parameter such as compare.
The utility model adopts the methyl alcohol evaporation gasification and the air preheating system of band reboiler, and methyl alcohol and air are heated respectively and measure, be convenient in the gas mixture component more accurately the amount of carrying out improved the reliability of system than compatibility.
The utility model has been cancelled overheated operation in the traditional technology, set up the quaternary gas mixer (Fig. 4) of band demister, make air, methyl alcohol, water vapor and tail gas obtain thorough mixing, created condition for enlarging oxygen-methanol ratio, usually oxygen-methanol ratio can be controlled in 0.43～0.45, and the common oxygen-methanol ratio of traditional technology is controlled at about 0.38～0.42, according to Le Chatelier's principle, improves oxygen-methanol ratio and can further improve reaction yield.
The utility model adopts fixed-bed type oxidizer (Fig. 3), it adopts the design of water-bath type tube sheet, tube sheet to adopt two ends to have the Asia flat pipe tube sheet (being the flat head that generally adopts in the boiler) of flexible radian, carry out integral solder after the skiving technology of passing through, generally adopt in the formaldehyde plant steam gas bag and reactor serial connection be designed to one.It can effectively prevent beds distortion, shorten reaction product in the residence time of high-temperature zone, have characteristics such as main reaction is effective, side reaction is few, long service life.
The catalyzer that the utility model adopts is high-purity crystallized silver, outward appearance is the dendritic gathering of coral, have high catalyst activity, good selectivity, stronger physical strength, thermostability and stronger poison resistance preferably, it is long therefore to install the cycle of operation, is generally 3～6 months.
The utility model has been set up middle trap (Fig. 5) and terminal trap (Fig. 6) in absorption system, reduced the escape of formaldehyde foam and droplet, has effectively reduced unit consumption, makes the absorption of formaldehyde improve more with efficient.Middle trap is that the riser of the separated space that forms of circular cone, purified gas discharge and particle drop are discharged four parts and constituted by tangential inlet, cylinder, gas flow in the device is a kind of double-deck eddy flow, nearly wall part is for being rotated down, claim outer eddy flow, centre portions is for rotating up, eddy flow in claiming, both rotation directions are identical.In the eddy flow, tangential velocity is occupied an leading position, and drives particle by its and does around device axle high speed rotary motion, thereby make particle and drop be thrown toward wall under centrifugal effect and be separated.The terminal trap is to be with the vertical cylindrical shell of tangential entry pipe to reach by one, following two cones are formed, the pipe of a upper end closed is set in cylinder center, in the annular space between pipe and outer cylinder body, some isocentric circular arc plate washers are housed, some conduits have been constituted, air-flow enters in the cylinder from the tangential entry pipe, be separated into some strands of air-flows by the circular arc plate washer, do to flow on the screw along conduit respectively, meet at the upper cone of equipment at last, discharge from the outlet pipe of top center, when air-flow is made helicoidal flow along conduit, the mist of carrying secretly in the air-flow or other molecule under centrifugal action, produce downward radial displacement, just defendant's adhesion when in a single day particulate bumps against the vertical panel face, form liquid film and be captured, flow into lower cone at last, discharge from the bottom leakage fluid dram.
Filtering material in the utility model strainer is selected for use efficiently, low-resistance and folding filtrate that can reverse gas cleaning, has improved the degree of purification of multicomponent raw material gas mixture.This filtering material has good filtration effect (can remove the above grit of 0.3 μ, removal effect can reach more than 99%,), characteristics such as filtration resistance is little, long service life, the collapsible filter bag of star that it adopts paper substrate, chemical fibre or film filtrate to make, its filtration area is about 20 to 30 times with the common filter bag of volume, because of it can adopt pulse backblowing and adverse current reverse gas cleaning, can reach 1 to 2 year work-ing life.
The utility model possesses iron molybdenum catalysis method technology to be produced the advantage of high-concentration formaldehyde and conventional silver legal system and gets that the formaldehyde technology investment is economized, advantage of low energy consumption, has reduced investment (only being iron molybdenum method 1/3 investment cost), can produce concentrated formaldehyde, formaldehyde Functionality, quality and appealing design, methyl alcohol unit consumption low (minimum unit consumption can reach 435Kg methyl alcohol/ton formaldehyde), low, easy and simple to handle, the practical characteristics of energy consumption.
(4) description of drawings
Fig. 1 produces the structural representation of formaldehyde plant for the utility model exhaust gas circulation process.
Fig. 2 produces the formaldehyde process flow diagram for the conventional silver catalysis method.
Fig. 3 is the cross-sectional view of fixed-bed type oxidizer in the utility model device.
Fig. 4 is the cross-sectional view of quaternary gas mixer in the utility model device.
Fig. 5 is the cross-sectional view of middle trap in the device for the utility model.
Fig. 6 is the cross-sectional view of terminal trap in the utility model device.
Among the figure: methanol pump 1, methyl alcohol strainer 2, air filter 3, tail gas gas blower 4, methyl alcohol reboiler 5, Root's blower 6, heater exhaust gas 7, methanol evaporator 8, airheater 9, quaternary gas mixer 10, vapor filter 11, vapour distributor 12, quaternary gas filter 13, fixed-bed type oxidizer 14, first absorption tower 15, middle trap 16, one column plate type interchanger 17, one tower recycle pump 18, second absorption tower 19, terminal trap 20, two column plate type interchanger II21, two tower recycle pump II22, two tower recycle pump I23, two column plate type interchanger I24, tail gas liquid seal trough 25, exhaust gas treating device 26.
(5) embodiment
Referring to Fig. 1, the exhaust gas circulation process that the utility model relates to is produced formaldehyde plant, mainly by methanol pump 1, methyl alcohol strainer 2, air filter 3, tail gas gas blower 4, methyl alcohol reboiler 5, Root's blower 6, heater exhaust gas 7, methanol evaporator 8, airheater 9, quaternary gas mixer 10, vapor filter 11, vapour distributor 12, quaternary gas filter 13, fixed-bed type oxidizer 14, first absorption tower 15, middle trap 16, one column plate type interchanger 17, one tower recycle pump 18, second absorption tower 19, terminal trap 20, two column plate type interchanger II21, two tower recycle pump II22, two tower recycle pump I23, two column plate type interchanger I24, tail gas liquid seal trough 25 and exhaust gas treating device 26 are formed.
Described methanol pump 1 discharge port links to each other with methyl alcohol strainer 2 opening for feeds, methyl alcohol strainer 2 discharge ports link to each other with methyl alcohol reboiler 5 bottoms, methyl alcohol reboiler 5 tops and 8 middle linking to each other of methanol evaporator, methanol evaporator 8 tops link to each other with 10 imports of quaternary gas mixer, and methanol evaporator 8 bottoms link to each other with methyl alcohol reboiler 5; Described air filter 3 outlets link to each other with Root's blower 6 imports, Root's blower 6 outlets link to each other with airheater 9 imports, airheater 9 outlets link to each other with 10 imports of quaternary gas mixer, vapour distributor 12 imports link to each other with fixed-bed type oxidizer 14 vapour outlets, vapour distributor 12 outlets link to each other with vapor filter 11 imports, and vapor filter 11 outlets link to each other with 10 imports of quaternary gas mixer; 4 outlets of tail gas gas blower link to each other with heater exhaust gas 7 imports, heater exhaust gas 7 outlets link to each other with 10 imports of quaternary gas mixer, 10 outlets of quaternary gas mixer link to each other with 13 imports of quaternary gas filter, 13 outlets of quaternary gas filter link to each other with 14 imports of fixed-bed type oxidizer, the gas-liquid mixture outlet of fixed-bed type oxidizer 14 links to each other with 15 imports of first absorption tower, 15 bottoms, first absorption tower link to each other with a tower recycle pump 18 imports, 18 outlets of one tower recycle pump link to each other with a column plate type interchanger 17 imports, 17 outlets of one column plate type interchanger divide two the tunnel, one the tunnel is connected with pipeline 27, another road absorbs additional liquid import with 15 tops, first absorption tower and links to each other, first absorption tower, 15 top exits link to each other with middle trap 16, middle trap 16 gaseous phase outlets link to each other with 19 imports of second absorption tower, middle trap 16 liquid phases outlet links to each other with 15 tops, first absorption tower, 19 bottoms, second absorption tower link to each other with two tower recycle pump I23 imports, two tower recycle pump I23 outlet links to each other with two column plate type interchanger I24 imports, two column plate type interchanger I24 outlet divides two the tunnel, one the tunnel links to each other with 19 middle parts, second absorption tower, another road links to each other with 15 bottoms, first absorption tower, two tower recycle pump II22 imports link to each other with 19 middle parts, second absorption tower, two tower recycle pump II22 outlet links to each other with two column plate type interchanger II21 imports, two column plate type interchanger II21 outlet replenishes the absorption liquid import with 19 tops, second absorption tower and links to each other, the 19 top tail gas outlets of second absorption tower link to each other with terminal trap 20, the outlet of terminal trap 20 tail gas divides two the tunnel, one the tunnel links to each other with tail gas liquid seal trough 25, tail gas liquid seal trough 25 links to each other with exhaust gas treating device 26, and another road links to each other with 4 imports of tail gas gas blower.
Methyl alcohol is squeezed into methyl alcohol reboiler 5 from methyl alcohol reboiler 5 bottoms by methanol pump 1 from the methyl alcohol scale tank after methyl alcohol strainer 2 filters; Simultaneously methyl alcohol reboiler 5 shell sides are by from drum and make methanol gasifying in the methyl alcohol reboiler through the heating steam heating of variable valve control (vaporization temperature is controlled at 78～82 ℃, evaporating pressure and is controlled at 70～80kpa) and enter methanol evaporator 8, methyl alcohol gas in the methanol evaporator 8 from the methanol evaporator top behind silk screen mist eliminator precipitation of liquid droplets, pipeline through having the steam heating sleeve pipe enters quaternary gas mixer 10, and the methanol solution pump around circuit in the methanol evaporator 8 is to methyl alcohol reboiler 5 bottoms; Send into airheater 9 from the air of air filter 3 by Root's blower 6, after airheater 9 heating (temperature is controlled at 108～112 ℃), enter quaternary gas mixer 10; Batching steam is regulated flow by variable valve from vapour distributor 12 and is entered quaternary gas mixer 10 after vapor filter 11 filters.After normal the driving, exhaust gas circulation system earlier with the tail gas displacement qualified after, the part tail gas of opening after tail gas gas blower 4 will heat through heater exhaust gas 7 be sent into quaternary gas mixer 10.Quaternary gas is uniform mixing in quaternary gas mixer 10, has in the fixed-bed type of the crystal silver catalyst oxidizer 14 through sending into to mat formation by spark arrester again after the quaternary gas filter 13 further excessively small amount of impurities that eliminations may have then.Oxidization of methanol and dehydrogenation reaction (temperature of reaction is controlled at 610～650 ℃) generation formaldehyde gas take place from top to bottom by the crystal silver catalyst layer in reactant gases under the effect of high temperature and catalyzer.For preventing the thermolysis of reaction product, the formaldehyde hot gas of generation rapidly by with fixed-bed type oxidizer 14 in quench zone carry out quenching (temperature after the quenching is lower than 200 ℃), send into then in the multistage absorption tower and absorb.The formaldehyde finished product is by the 15 bottom extraction of first absorption tower, and the additional process water that is used to absorb formaldehyde gas is by the adding of 19 tops, second absorption tower, and technology soft water adds fixed-bed type oxidizers 14 useless pot sections from pipeline 28.The formaldehyde solution of 15 bottoms, first absorption tower is got through a column plate type interchanger 17 cooling back (first absorbs column bottom temperature is controlled at＜80 ℃, cat head＜35 ℃) the one tunnel with a tower recycle pump 18 and is beaten to product intermediate storage tank as formaldehyde products through pipeline 27, and one the tunnel beats to 15 tops, first absorption tower as absorbing additional liquid.Rare aldehyde liquid at the bottom of 19 towers of second absorption tower is got through two column plate type interchanger I24 cooling back (the second absorption column bottom temperature is controlled at＜60 ℃, cat head＜40 ℃) a tunnel with two tower recycle pump I23 and is circulated back to 19 middle parts, second absorption tower and absorbs the formaldehyde gas that first absorption tower 15 has not absorbed, and another part is sent into 15 bottoms, first absorption tower and is used for reducing the liquidus temperature of 15 bottoms, first absorption tower.Draw time rare formaldehyde of lower concentration from 19 middle parts, second absorption tower and after two column plate type interchanger II21 cooling, send into 19 tops, second absorption tower absorption liquid as a supplement with two tower recycle pump II22.Formaldehyde gas carries out counter current contact with absorption liquid (absorption liquid is for flowing to) from top to bottom from bottom to top after entering first absorption tower 15, gas-liquid can fully be contacted, gas dissolving is to absorption liquid, be not absorbed on first absorption tower 15 that trap 16 carries out the gas-liquid shunting in the middle of gas enters from first absorption tower, 15 top exits completely, entrained drip or liquid phase foam enter second absorption tower 19 in the prevention gas phase influences assimilation effect, liquid-phase reflux is to 15 tops, first absorption tower, gas phase enters the 19 bottom gas phase imports of second absorption tower, gas moves from bottom to top and absorbs once more, the unabsorbed tail gas in 19 tops, second absorption tower is after terminal trap 20 separates moisture, one the tunnel sends in the exhaust gas treating device 26 burning (exhaust gas treating device fire box temperature be controlled at＜700 ℃) after tail gas liquid seal trough 25 usefulness fresh waters absorb once more, liberated heat is used for producing indirectly water vapor, and this part steam mainly uses for outside; Another road tail gas carries out the tail gas circulation via 4 pressurizations of tail gas gas blower after heater exhaust gas 7 heating enter production system, part or whole water vapor are as the thermo-stabilizer of reaction heat in the alternative traditional technology of this part tail gas, form the quaternary gas mixture with methyl alcohol, air and steam, can produce the formaldehyde solution of different concns according to customer requirements, general concentration of formaldehyde can be controlled 37%～55%.
Can find that from the above description the utility model device can reach following technique effect:
1, can produce low alcohol (＜1%), low acid (＜0.01%), low unit consumption (1 ton of first of every production 435 kilograms of the minimum consumption methyl alcohol of aldehyde), high-concentration formaldehyde (content of formaldehyde 37%～55%).
2, the safe and stable arrangement cycle of operation long, device is not less than 3 months the uptime, and is the longest Can reach 6 months.
3, quaternary filter filtering material can clean repeatedly, generally can use 1～2 year.
4, production operation safety coefficient is higher, the device design is more reasonable, floor space is littler, device Be constructed and put into operation rear maintenance still less, the investment still less.
5, the energy synthesis recycling is more abundant, and 1 ton of formaldehyde of every production is satisfying self device operation Condition under can be outward for 0.305 ton of 0.5Mpa steam.
Claims (1)
1, a kind of exhaust gas circulation process is produced formaldehyde plant, it is characterized in that described device comprises methanol pump (1), methyl alcohol strainer (2), air filter (3), tail gas gas blower (4), methyl alcohol reboiler (5), Root's blower (6), heater exhaust gas (7), methanol evaporator (8), airheater (9), quaternary gas mixer (10), vapor filter (11), vapour distributor (12), quaternary gas filter (13), fixed-bed type oxidizer (14), first absorption tower (15), middle trap (16), one column plate type interchanger (17), one tower recycle pump (18), second absorption tower (19), terminal trap (20), two column plate type interchanger II (21), two tower recycle pump II (22), two tower recycle pump I (23), two column plate type interchanger I (24), tail gas liquid seal trough (25) and exhaust gas treating device (26), described methanol pump (1) discharge port links to each other with methyl alcohol strainer (2) opening for feed, methyl alcohol strainer (2) discharge port links to each other with methyl alcohol reboiler (5) bottom, methyl alcohol reboiler (5) top links to each other with methanol evaporator (8) is middle, methanol evaporator (8) top links to each other with quaternary gas mixer (10) import, and methanol evaporator (8) bottom links to each other with methyl alcohol reboiler (5); Described air filter (3) outlet links to each other with Root's blower (6) import, Root's blower (6) outlet links to each other with airheater (9) import, airheater (9) outlet links to each other with quaternary gas mixer (10) import, vapour distributor (12) import links to each other with fixed-bed type oxidizer (14) vapour outlet, vapour distributor (12) outlet links to each other with vapor filter (11) import, and vapor filter (11) outlet links to each other with quaternary gas mixer (10) import; Tail gas gas blower (4) outlet links to each other with heater exhaust gas (7) import, heater exhaust gas (7) outlet links to each other with quaternary gas mixer (10) import, quaternary gas mixer (10) outlet links to each other with quaternary gas filter (13) import, quaternary gas filter (13) outlet links to each other with fixed-bed type oxidizer (14) import, the gas-liquid mixture outlet of fixed-bed type oxidizer (14) links to each other with first absorption tower (15) import, bottom, first absorption tower (15) links to each other with tower recycle pump (a 18) import, the outlet of one tower recycle pump (18) links to each other with column plate type interchanger (a 17) import, the outlet of one column plate type interchanger (17) divides two the tunnel, one the tunnel is connected with pipeline (27), another road absorbs additional liquid import with top, first absorption tower (15) and links to each other, first absorption tower (15) top exit links to each other with middle trap (16), middle trap (16) gaseous phase outlet links to each other with second absorption tower (19) import, middle trap (16) liquid phase outlet links to each other with top, first absorption tower (15), bottom, second absorption tower (19) links to each other with two tower recycle pump I (23) imports, two tower recycle pump I (23) outlet links to each other with two column plate type interchanger I (24) imports, two column plate type interchanger I (24) outlet divides two the tunnel, one the tunnel with second absorption tower (19) middle part link to each other, another road links to each other with first absorption tower (15) bottom, two tower recycle pump II (22) imports link to each other with second absorption tower (19) middle part, two tower recycle pump II (22) outlet links to each other with two column plate type interchanger II (21) imports, two column plate type interchanger II (21) outlet replenishes the absorption liquid import with top, second absorption tower (19) and links to each other, the tail gas outlet of top, second absorption tower (19) links to each other with terminal trap (20), the outlet of terminal trap (20) tail gas divides two the tunnel, one the tunnel links to each other with tail gas liquid seal trough (25), tail gas liquid seal trough (25) links to each other with exhaust gas treating device (26), and another road links to each other with tail gas gas blower (4) import.
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| CNU2008201599655U CN201305565Y (en) | 2008-09-24 | 2008-09-24 | Device for preparing formaldehyde by exhaust gas circulation process |
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Cited By (12)
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| CN102391082A (en) * | 2011-09-07 | 2012-03-28 | 安徽金禾实业股份有限公司 | Method and device for heat exchange of methanol in production of formaldehyde |
| CN104667694A (en) * | 2015-03-25 | 2015-06-03 | 南通江天化学股份有限公司 | Methanol purification device in iron-molybdenum-process formaldehyde production process |
| CN105294414A (en) * | 2015-11-19 | 2016-02-03 | 安徽中源化工有限公司 | Formaldehyde production system |
| CN105732342A (en) * | 2016-03-25 | 2016-07-06 | 湖北三江化工有限责任公司 | Formaldehyde production method based on exhaust gas circulating process |
| CN106083541A (en) * | 2016-06-03 | 2016-11-09 | 滁州市龙飞化工有限公司 | A kind of method utilizing silver catalytic oxidation to prepare formaldehyde |
| CN107056593A (en) * | 2017-02-17 | 2017-08-18 | 唐山中浩化工有限公司 | A kind of production method and system of ultra-large formaldehyde |
| CN107200682A (en) * | 2017-07-12 | 2017-09-26 | 广东奕宏化工有限公司 | A kind of improved Formaldehyde Production system |
| CN107311848A (en) * | 2017-07-12 | 2017-11-03 | 安徽弘源化工科技有限公司 | One kind bypass oxygenation type formaldehyde preparation system |
| CN109232217A (en) * | 2018-11-08 | 2019-01-18 | 山东明化新材料有限公司 | A kind of flue gas recirculation prepn. of formaldehyde and its device |
| CN110563903A (en) * | 2019-09-06 | 2019-12-13 | 无锡市华立石化工程有限公司 | preparation system and preparation process of urea formaldehyde pre-condensed liquid |
| US10538476B2 (en) * | 2015-03-24 | 2020-01-21 | Johnson Matthey Davy Technologies Limited | Process for carrying out a reaction in a reaction column |
| CN110759823A (en) * | 2019-09-23 | 2020-02-07 | 扬州市众鑫化工有限公司 | Preparation method of low-concentration formaldehyde solution for water-based binder |
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- 2008-09-24 CN CNU2008201599655U patent/CN201305565Y/en not_active Expired - Fee Related
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102391082B (en) * | 2011-09-07 | 2013-08-14 | 安徽金禾实业股份有限公司 | Method and device for heat exchange of methanol in production of formaldehyde |
| CN102391082A (en) * | 2011-09-07 | 2012-03-28 | 安徽金禾实业股份有限公司 | Method and device for heat exchange of methanol in production of formaldehyde |
| US10538476B2 (en) * | 2015-03-24 | 2020-01-21 | Johnson Matthey Davy Technologies Limited | Process for carrying out a reaction in a reaction column |
| CN104667694A (en) * | 2015-03-25 | 2015-06-03 | 南通江天化学股份有限公司 | Methanol purification device in iron-molybdenum-process formaldehyde production process |
| CN105294414A (en) * | 2015-11-19 | 2016-02-03 | 安徽中源化工有限公司 | Formaldehyde production system |
| CN105732342A (en) * | 2016-03-25 | 2016-07-06 | 湖北三江化工有限责任公司 | Formaldehyde production method based on exhaust gas circulating process |
| CN106083541A (en) * | 2016-06-03 | 2016-11-09 | 滁州市龙飞化工有限公司 | A kind of method utilizing silver catalytic oxidation to prepare formaldehyde |
| CN107056593A (en) * | 2017-02-17 | 2017-08-18 | 唐山中浩化工有限公司 | A kind of production method and system of ultra-large formaldehyde |
| CN107311848A (en) * | 2017-07-12 | 2017-11-03 | 安徽弘源化工科技有限公司 | One kind bypass oxygenation type formaldehyde preparation system |
| CN107200682A (en) * | 2017-07-12 | 2017-09-26 | 广东奕宏化工有限公司 | A kind of improved Formaldehyde Production system |
| CN109232217A (en) * | 2018-11-08 | 2019-01-18 | 山东明化新材料有限公司 | A kind of flue gas recirculation prepn. of formaldehyde and its device |
| CN110563903A (en) * | 2019-09-06 | 2019-12-13 | 无锡市华立石化工程有限公司 | preparation system and preparation process of urea formaldehyde pre-condensed liquid |
| CN110759823A (en) * | 2019-09-23 | 2020-02-07 | 扬州市众鑫化工有限公司 | Preparation method of low-concentration formaldehyde solution for water-based binder |
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