CN2048064U - Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower - Google Patents
Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower Download PDFInfo
- Publication number
- CN2048064U CN2048064U CN 89212109 CN89212109U CN2048064U CN 2048064 U CN2048064 U CN 2048064U CN 89212109 CN89212109 CN 89212109 CN 89212109 U CN89212109 U CN 89212109U CN 2048064 U CN2048064 U CN 2048064U
- Authority
- CN
- China
- Prior art keywords
- pipe
- gas
- tube bundle
- cooler tube
- basket
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 32
- 238000010276 construction Methods 0.000 title abstract description 7
- 239000007789 gas Substances 0.000 claims abstract description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 11
- 239000000618 nitrogen fertilizer Substances 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 230000003197 catalytic effect Effects 0.000 claims description 23
- 239000010410 layer Substances 0.000 claims description 17
- 239000001257 hydrogen Substances 0.000 claims description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims description 12
- 229910000831 Steel Inorganic materials 0.000 claims description 11
- 239000010959 steel Substances 0.000 claims description 11
- 238000009413 insulation Methods 0.000 claims description 9
- 239000000945 filler Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 235000007164 Oryza sativa Nutrition 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 235000009566 rice Nutrition 0.000 claims description 4
- 241000196324 Embryophyta Species 0.000 claims description 3
- 239000011229 interlayer Substances 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 235000012149 noodles Nutrition 0.000 claims description 3
- 230000000284 resting effect Effects 0.000 claims description 3
- 125000006850 spacer group Chemical group 0.000 claims description 3
- 239000012190 activator Substances 0.000 claims description 2
- 210000004907 gland Anatomy 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 150000002431 hydrogen Chemical class 0.000 claims description 2
- 210000002445 nipple Anatomy 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims description 2
- 240000007594 Oryza sativa Species 0.000 claims 1
- 239000003337 fertilizer Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 claims 1
- 239000003054 catalyst Substances 0.000 abstract description 17
- 230000015572 biosynthetic process Effects 0.000 abstract description 6
- 238000012423 maintenance Methods 0.000 abstract description 5
- 238000003786 synthesis reaction Methods 0.000 abstract description 5
- 238000011068 loading method Methods 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 241000209094 Oryza Species 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 1
- 206010063493 Premature ageing Diseases 0.000 description 1
- 208000032038 Premature aging Diseases 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 239000003566 sealing material Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to an internal construction member of cocurrent flow gas-distributing ammonia synthetic tower for the manufacture of nitrogenous fertilizer, which is used for ammonia synthesis in medium and small size nitrogenous fertilizer plant. The internal construction member of cocurrent flow gas-distributing ammonia synthetic tower adopts a round flat cold pipe bundle [8]. Unreacted hydrogen gas and nitrogen gas is directly introduced into the cold pipe bundle to cool the thermal gas which is generated by the reaction of catalyst bed. The cold pipe bundle can make the structure simplified, increase the charge of catalyst and also reduce the height and dimension of the recuperator [1]. The volume utilization coefficient of the high-pressure containers is improved from 43-45% in the prior art to 59.6%. As compared with the internal construction member of the native synthetic tower with the same dimension, the ability of producing ammonia increases about 30%. At the same time, the whole cold pipe bundle which can be taken out is convenient for maintenance. The utility model has the advantages of easy loading and unloading of the catalyst, lower manufacture cost and operating cost of the internal component than that of the existing synthetic tower.
Description
A kind of cocurrent flow type gas-distributing type ammonia converter internals that relates to nitrogen fertilizer production technical process and equipment is used for the synthetic of medium and small nitrogen fertilizer plant ammonia, belongs to nitrogen fertilizer production equipment.
Existing middle-size and small-size nitrogen fertilizer plant ammonia synthesis converter cooling pipe type internals commonly used have and flows two kinds of pair telescopings and single tube cocurrent flow types.It mainly partly forms i.e. catalytic bed (including cooler tube bundle), and interchanger by two.The technical process of this internals is: whole unreacted hydrogen nitrogen cold air reacted hot gas in heat transfer tube outer wall and inside pipe wall exchanges, cold air is heated to 350～380 ℃ in the heat exchanging process of interchanger, upcast through cooler tube bundle arrives cooler tube bundle again, from top to bottom heated once more by the hot gas (being synthetic gas) of the outer catalytic bed of pipe, temperature reaches 400～430 ℃ of upper ends that enter pipe core and enters catalytic bed again, in bed, from top to bottom, carry out the thermopositive reaction of ammonia synthesis.Reaction back gaseous ammonia content increases by 8～11%, and temperature is increased to 410～430 ℃, leaves the catalyst bed outside interchanger cooling back discharge tower, thereby finishes the process of ammonia synthesis.
There are many problems in existing ammonia converter internals (referring to Fig. 4) on structure and technology, as everyone knows, the size of ammonia synthesis converter synthetic ammonia ability is relevant with many factors, in same volume, the catalyst of filling is many more, the synthetic ammonia ability is just big more, and the heat exchanger height of existing synthetic ammonia tower inner parts is generally more than 1.8 meters, the height dimension of cooler tube bundle is bigger, also has gas distributor in addition, occupy segment space, cause the volume utilization coefficient in the high pressure vessel to have only 43～45%, the loadings of catalyst is less relatively.Simultaneously, because of the scantlings of the structure of interchanger and cooler tube bundle is bigger, cause the synthetic ammonia gas reaction to depart from the optimum temps zone.Because tube bank is welded construction with parts such as cylindrical shell, internals are damaged easily, and after damaging, need the inner core cutting could be repaired, maintenance difficult, cost height, internals weak point in work-ing life, problem such as current consumption is big.
The purpose of this utility model just is to provide a kind of volumetric efficiency height, big, the cold and hot gas converting heat of catalyst filling amount effective, and cooler tube bundle is convenient to maintenance and inspection, and temperature of reaction occupy the cocurrent flow type gas-distributing type ammonia converter internals in the best region.
The utility model divides streamed by gas, unreacted hydrogen and nitrogen gas body is main partly outer by after the heating of the hot gas of inner reaction tube through interchanger, directly enters the catalyst bed via pipe core.Another part temperature is that 30～100 ℃ gas heats without interchanger, from top to bottom bed is cooled off and directly enter cooler tube bundle by cat head through airway, come out the gas of preheating via two upcasts and through interchanger from cold pipe, and mix by the gas after the pipe core heat exchange and to enter catalytic bed again and down react, can make the cold and hot gas temperature difference big, heat-transfer capability is strong, the temperature that both can make catalytic bed is by the optimum temps curve distribution, unreacted gas is fully heated, the heat exchange efficiency height, can reduce the height of cooler tube bundle on the one hand, can dwindle heat exchanger volume again on the other hand, thereby the volume utilization coefficient in the high pressure vessel is brought up to more than 59%.The loadings of catalyzer can correspondingly increase, and the synthetic of ammonia can carry out in the optimum temps zone, and reaction heat energy in time shifts out, tube bank simultaneously is the circle flat, and tube bank is a removable structure with cylindrical shell, and tube bank can wholely be taken out, keep in repair very conveniently, realize its purpose by above-mentioned measure.
Below in conjunction with drawings and Examples in detail, principle of work of the present utility model and constitutional features are described in detail.
Description of drawings:
Fig. 1 is a main sectional view of the present utility model.
Fig. 2 is a basket sectional view of the present utility model.
Fig. 3 is an interchanger sectional view of the present utility model.
Fig. 4 uses the wider two telescoping synthetic towers of also stream in the prior art.
Fig. 4 is the two telescoping synthetic towers of using always in the prior art of also stream, and this ammonia converter internals is old-fashioned, and the cooler tube bundle in basket is circular tube structure, is provided with gas distributor, and whole interchanger size is bigger, and the parts on tube bank and the cylindrical shell are welded construction.It is mainly by four-way ［ 01 ］, carriage ［ 02 ］, bottom ［ 03 ］, card ［ 04 ］, heat transfer tube ［ 05 ］, outer cylinder body ［ 06 ］, baffle plate ［ 07 ］, cold looped pipeline ［ 08 ］, gas distributor ［ 09 ］, thermocouple well ［ 010 ］, cooling jacket ［ 011 ］, and pipe core ［ 012 ］, electric heater ［ 013 ］, top cover ［ 015 ］ etc. are formed.Unreacted hydrogen and nitrogen gas body is entered by the top inlet mouth of synthetic tower, behind the annular space between inside and outside tube by the bottom of the tower interchanger of flowing through, flow to gas distributor ［ 09 ］ then, again through cooling jacket ［ 011 ］, pipe core ［ 012 ］, enter the reaction of catalytic bed and activator, reacted synthetic ammonia gas via Tube Sheet of Heat Exchanger ［ 05 ］ after, discharge outside the tower.
Fig. 1 is a main sectional view of the present utility model, and ammonia converter internals mainly is building-up reactions and the partly heat exchange of carrying out the hydrogen and nitrogen gas body in basket by basket ［ 2 ］ and interchanger ［ 1 ］ two most formation, and gas synthetic reaction heat energy is in time shifted out.Interchanger mainly is the heat exchange of hot and cold gas, and synthetic ammonia gas flows out behind interchanger outside the tower, carries out next process.
Fig. 2 is the sectional view of the utility model basket, and it is mainly by cylindrical shell pipe nipple ［ 3 ］, lower face plate ［ 4 ］, following silk screen ［ 5 ］, support bar sleeve pipe ［ 6 ］, location pipe support ［ 7 ］, cooler tube bundle ［ 8 ］, spacer ［ 9 ］, backing ring ［ 10 ］, interlayer silk screen ［ 11 ］, little bucket ［ 12 ］, resting support ［ 13 ］, last silk screen ［ 14 ］, stuffing box ［ 15 ］, top cover ［ 16 ］, shell flange ［ 17 ］, wear ring ［ 18 ］, short tube ［ 19 ］, short cover ［ 20 ］, refrigerator pipe ［ 21 ］, brachymedial core barrel ［ 22 ］, muff ［ 23 ］, hold-down nut ［ 24 ］, upcast ［ 25 ］ basket sheath ［ 26 ］, thermal insulation layer ［ 27 ］, basket cylindrical shell ［ 28 ］, pipe core ［ 29 ］, thermopair ［ 30 ］, directed sleeve pipe ［ 31 ］, double-screw bolt ［ 32 ］, thermal insulation layer compositions such as ［ 34 ］.
In basket ［ 2 ］, unreacted hydrogen and nitrogen gas body and reacted synthetic ammonia gas carry out heat exchange, and the hydrogen and nitrogen gas body carries out the synthetic of ammonia under the katalysis of catalyst simultaneously.Basket ［ 2 ］ is installed in the circular basket cylindrical shell ［ 28 ］, is incubated with lagging material, thermal insulation layer ［ 27 ］ is set, makes basket sheath ［ 26 ］ in the outside of thermal insulation layer with metallic substance.In order to measure temperature in the basket, thermopair ［ 30 ］ is set, it is inserted in the directed sleeve pipe ［ 30 ］.And directional catheter ［ 31 ］ is installed on the lower face plate ［ 4 ］.
Cooler tube bundle ［ 8 ］ as the heat exchanger in the catalytic bed, it is installed in the middle part of basket, every cold pipe of cooler tube bundle ［ 8 ］, two ends are pipe, every end length is 150～200mm, the centre is a flat tube, on cooler tube bundle has, following volute is communicated with each other, air-flow is heated from top to bottom, three supporting bars are arranged at the bottom of cooler tube bundle, and it is positioned at respectively in the support bar sleeve pipe ［ 6 ］, and supporting tube sleeve pipe ［ 6 ］ is bearing on the lower face plate ［ 4 ］, the upper end of cooler tube bundle ［ 8 ］ has two airways to be inserted in the stuffing box ［ 15 ］, so the equal retractable in two ends of cooler tube bundle ［ 8 ］.Owing in stuffing box ［ 15 ］ and other stuffing box, all adopt expanded graphite to make filler, can make fitting piece maintenance good air-tightness in the stuffing box, improved the reliability of whole synthetic tower.The position of cooler tube bundle ［ 8 ］ is fixed by location pipe support ［ 7 ］, support bar sleeve pipe ［ 6 ］ and stuffing box.Unreacted hydrogen and nitrogen gas body directly enters cooler tube bundle ［ 8 ］ by refrigerator pipe ［ 21 ］, is used for cooling off catalytic bed.Last silk screen ［ 14 ］ and resting support ［ 13 ］ are bearing in the upper end of pipe core ［ 29 ］ and use hold-down nut ［ 24 ］ fastening, interlayer silk screen ［ 11 ］ is bearing on the backing ring ［ 10 ］, pipe core ［ 29 ］ is then supported by the connection base ［ 49 ］ on the interchanger ［ 1 ］, be installed on the upper tubesheet ［ 48 ］ and connect base ［ 49 ］, between the upper and lower silk screen layer catalyst is housed, hydrogen-nitrogen mixture gas just reacts in this section, this section is referred to as catalytic bed, at zero rice, top of catalytic bed, the mouth of pipe of pipe core ［ 29 ］ and upcast ［ 25 ］ extends this place.Outwards propagate for preventing the heat in the basket, muff ［ 23 ］ is arranged at the top of basket ［ 2 ］, top cover ［ 16 ］ is arranged at the top of muff ［ 23 ］, top cover ［ 16 ］ is inlaid in the interior circle of shell flange ［ 17 ］, stuffing box ［ 15 ］ is installed on the top cover ［ 16 ］, with wear ring ［ 18 ］ welded seal, in case internals need to repair, as long as wear ring ［ 18 ］ is blown off, whole cooler tube bundle just can take out maintenance.
Cold air enters cooler tube bundle by refrigerator pipe ［ 21 ］ through the airway of cooler tube bundle ［ 8 ］, flow from top to down, flow out from upcast ［ 25 ］ behind the volute of bottom, cold air temperature at this moment is heated to 350～400 ℃ again, and it directly enters catalytic bed.Another strand gas enters catalytic bed through the upper end of pipe core ［ 29 ］ after being heated from interchanger ［ 1 ］, carry out the thermopositive reaction of synthetic ammonia.Reacted gas is discharged outside the tower through the aperture of lower face plate ［ 4 ］ and the tubulation ［ 24 ］ in the interchanger ［ 1 ］, steel pipe ［ 62 ］ and is entered next process.
Last silk screen layer ［ 14 ］ only carries out the thermopositive reaction of synthetic ammonia gas to this section of cooler tube bundle ［ 8 ］ upper end, and therefore no heat exchange is called upper thermal insulating layer.This section of the lower end of cooler tube bundle ［ 8 ］ and following silk screen ［ 5 ］ is carried out the thermopositive reaction of synthetic ammonia equally, does not also have heat exchange with cooler tube bundle ［ 8 ］, and this section is called lower thermal insulating layer.The height of lower thermal insulating layer is 20～24% of a whole catalytic bed height, because cooler tube bundle ［ 8 ］ adopts the circle flat tube configuration, therefore the heat interchanging area of cold pipe ［ 8 ］ reduces, its shared volume also reduces, the catalyst filling amount is increased, and also flowing two telescoping synthetic tower (referring to Fig. 4) catalyst filling amounts in the prior art is 1.38m
3, the loadings of this device can reach 1.658m
3, cold pipe area/catalyst filling amount the utility model is 12.8m
2/ m
3, and prior art is 13.4m
2/ m
3, this is that the utility model is compared superior part with conventional art.
Fig. 3 is the sectional view of the utility model interchanger, the major function of interchanger is to carry out heat exchange, it and basket weldering are for one, mainly by packing gland ［ 35 ］, filler ［ 36 ］, filler seat ［ 37 ］, distance plate ［ 38 ］, inlet mouth ［ 39 ］, steel pipe ［ 40 ］, lower tubesheet ［ 41 ］, tubulation ［ 42 ］, urceolus ［ 43 ］, thermal insulation layer ［ 44 ］, big baffle plate ［ 45 ］, small front apron ［ 46 ］, steel loop ［ 47 ］, upper tubesheet ［ 48 ］, connect base ［ 49 ］, nut ［ 50 ］, pull bar ［ 51 ］, spacing tube ［ 52 ］, inner core ［ 53 ］, torispherical head ［ 54 ］, conical head ［ 55 ］, gusset ［ 56 ］, set collar ［ 57 ］, base ［ 58 ］, steel pipe ［ 59 ］, distance plate ［ 60 ］, pay inlet pipe ［ 61 ］, steel pipe ［ 62 ］ is formed.It is straight-through with pipe core ［ 29 ］ to pay inlet pipe ［ 61 ］, the top of pipe core ［ 29 ］ connects the zero rice noodles of catalytic bed, when temperature of reaction in the catalytic bed is too high, pay inlet pipe ［ 61 ］ and can supply with a part of unreacted hydrogen and nitrogen gas body, to regulate the temperature at catalytic bed zero rice noodles place, prevent to cause the catalyst premature aging and to the damage of internals because of temperature of reaction is too high.Cold air heated hydrogen and nitrogen gas body in interchanger ［ 1 ］ of paying inlet pipe ［ 61 ］ mixes in pipe core ［ 29 ］, be arranged with big baffle plate ［ 45 ］ in parallel with lower tubesheet ［ 41 ］ in the heat exchange ［ 1 ］, little plate washer ［ 46 ］, impel cold and hot gas in interchanger ［ 1 ］, fully to carry out heat exchange, cold air temperature is heated to more than 350 ℃, owing in design, cooler tube bundle ［ 8 ］ has been done bigger change, therefore the height dimension of interchanger ［ 1 ］ is reduced to below 0.8 meter by original 1.8 meters, the size of tubulation ［ 42 ］ changes φ 6.5 * 1.5 into by original φ 8 * 1.5, effective heat exchange area is strengthened, improved the volumetric efficiency of internals.Synthetic ammonia gas comes out from basket ［ 2 ］, enters the inner chamber of torispherical head ［ 54 ］ through tubulation ［ 42 ］, then from inner chamber through paying the annular space outflow between inlet pipe ［ 61 ］ and the steel pipe ［ 62 ］.Jia Re hydrogen and nitrogen gas body does not enter from inlet mouth ［ 39 ］, annular space between base ［ 58 ］ and steel pipe ［ 59 ］ flows out outside the tower, for guaranteeing that gas is not short-circuited with airtight, all fillers all adopt expanded graphite to make sealing material, the outer pipe of turnover tower all is provided with stuffing box, and stuffing box ［ 15 ］ is exactly like this.Be provided with thermal insulation layer ［ 44 ］ between urceolus ［ 43 ］ and the inner core ［ 53 ］.Urceolus ［ 43 ］ and conical head ［ 55 ］ weldering are welded with gusset ［ 56 ］ and are used for supporting conical head ［ 55 ］ for one in the bottom of conical head ［ 55 ］, whole internals are supported by base ［ 58 ］.After adopting the utility model, improve 2～3%, compare with old-fashioned unidimensional internals and produce ammonia ability increase about 30%, and required circulating flow rate is few, power consumption is little through the test ammonia net value.
The utility model main technical details:
Volume utilization coefficient: 59.6%
Catalyst filling amount: 1.68m
3
Cold pipe area/catalyst filling amount 12.8m
2/ m
3
Heat interchanging area/catalyst filling amount 19.6m
2/ m
3
Claims (6)
1, a kind of cocurrent flow type gas-distributing type synthetic ammonia tower inner parts that relates to chemical fertilizers production, be used for the synthetic of middle-size and small-size nitrogen fertilizer plant ammonia, it is made of basket and interchanger two major parts, it is characterized in that basket [2] is mainly by cylindrical shell pipe nipple [3], lower face plate [4], following silk screen [5], support bar sleeve pipe [6], location pipe support [7], cooler tube bundle [8], spacer [9], backing ring [10], interlayer silk screen [11], little bucket [12], resting support [13], last silk screen [14], stuffing box [15], top cover [16], shell flange [17], wear ring [18], short tube [19], short cover [20], refrigerator pipe [21], brachymedial core barrel [22], muff [23], hold-down nut [25], basket sheath [26], thermal insulation layer [27], basket cylindrical shell [28], pipe core [29], thermopair [30], directed sleeve pipe [31], bolt [32], muff [33], thermal insulation layer [34] is formed, interchanger [1] is mainly by packing gland [35], filler [36], filler seat [37], distance plate [38], inlet mouth [39], steel pipe [40], lower tubesheet [41], tubulation [42], urceolus [43], thermal insulation layer [44], big baffle plate [45], small front apron [46], steel loop [47], upper tubesheet [48], connect base [49], nut [50], pull bar [51], spacing tube [52], inner core [53], torispherical head [54], conical head [55], gusset [56], set collar [57], base [58], steel pipe [59], distance plate [60], pay inlet pipe [61], steel pipe [62] is formed, basket [2] is positioned at the top of interchanger [1], both welderings are one, temperature is to flow to cooler tube bundle [8] again 30～100 ℃ hydrogen nitrogen cold air is entered the straight tube of cooler tube bundle [8] upper end by refrigerator pipe [21] after, flow from top to down, the hydrogen and nitrogen gas body that is entered after the heating of catalytic bed and pipe core [29] by the upper end of upcast [25] carries out the synthetic of ammonia gas jointly in basket [2] again, the area of cooler tube bundle [8] is 12～14 with the ratio of activator volume, directly introduces the hot gas that cold air cools off the catalytic bed internal reaction by refrigerator pipe [21].
2, cocurrent flow type gas-distributing type synthetic ammonia tower inner parts according to claim 1, it is characterized in that cooler tube bundle ［ 8 ］ is positioned at the middle part of catalytic bed, locate with spacer ［ 9 ］ and location pipe support ［ 7 ］, and be inserted in the support bar sleeve pipe ［ 6 ］, be bearing on the lower face plate ［ 4 ］ by three supporting bars, there are two air guide straight tubes the upper end of cooler tube bundle ［ 8 ］, straight tube is stretched and is inserted in the stuffing box ［ 15 ］, is " free style " stretching structure.
3, according to claim 1 and 2 described cooler tube bundles ［ 8 ］, it is characterized in that the cold Guan Weiyuan flat pipe of cooler tube bundle, two ends are the long pipe of 150～200mm, middle flat tube for being pressed into, the two ends of pipe and upper and lower cylinder are linked up.
4, cocurrent flow type gas-distributing type synthetic ammonia tower inner parts according to claim 1, it is characterized in that silk screen ［ 14 ］ to this section of cooler tube bundle ［ 8 ］ upper end is upper thermal insulating layer, this section of silk screen under the type of cooler tube bundle ［ 8 ］ lower end, be lower thermal insulating layer, the height of lower thermal insulating layer is 20～24% of a whole catalytic bed height.
5, according to the described cocurrent flow type gas-distributing type of claim 1 synthetic ammonia tower inner parts, it is characterized in that pair inlet pipe ［ 61 ］, the cold air that are provided with straight-through catalytic bed in the interchanger ［ 1 ］ can directly lead to pipe core ［ 29 ］ to catalytic bed, to regulate the temperature at catalytic bed zero rice noodles place.
6, cocurrent flow type gas-distributing type synthetic ammonia tower inner parts according to claim 1, the filler and the filler ［ 36 ］ that it is characterized in that filling out in the letter ［ 15 ］ are expanded graphite, i.e. soft graphite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89212109 CN2048064U (en) | 1989-01-31 | 1989-01-31 | Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89212109 CN2048064U (en) | 1989-01-31 | 1989-01-31 | Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2048064U true CN2048064U (en) | 1989-11-22 |
Family
ID=4868297
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 89212109 Expired - Lifetime CN2048064U (en) | 1989-01-31 | 1989-01-31 | Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2048064U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102688734A (en) * | 2012-06-29 | 2012-09-26 | 石家庄工大化工设备有限公司 | Coal-made natural gas reactor |
| CN102704699A (en) * | 2012-05-24 | 2012-10-03 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN111548364A (en) * | 2020-05-22 | 2020-08-18 | 江西宏柏新材料股份有限公司 | Synthesis method and device of phenyl chlorosilane |
| CN119733445A (en) * | 2024-12-10 | 2025-04-01 | 山东赛诺凯特氢氨新能源有限公司 | A YHL synthesis tower, YHL preparation system and YHL green ammonia synthesis method for photovoltaic wind power generation hydrogen production and green ammonia synthesis |
-
1989
- 1989-01-31 CN CN 89212109 patent/CN2048064U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102704699A (en) * | 2012-05-24 | 2012-10-03 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN102704699B (en) * | 2012-05-24 | 2014-10-15 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN102688734A (en) * | 2012-06-29 | 2012-09-26 | 石家庄工大化工设备有限公司 | Coal-made natural gas reactor |
| CN111548364A (en) * | 2020-05-22 | 2020-08-18 | 江西宏柏新材料股份有限公司 | Synthesis method and device of phenyl chlorosilane |
| CN119733445A (en) * | 2024-12-10 | 2025-04-01 | 山东赛诺凯特氢氨新能源有限公司 | A YHL synthesis tower, YHL preparation system and YHL green ammonia synthesis method for photovoltaic wind power generation hydrogen production and green ammonia synthesis |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4732918A (en) | Heat interchanging process and reactor therefor | |
| WO2016119224A1 (en) | Isothermal and low temperature shift converter and shift conversion process thereof | |
| CN207153662U (en) | A kind of isothermal change furnace | |
| CN109850918A (en) | A kind of reactors for synthesis of ammonia and technique | |
| CN1088618C (en) | Improved catalytic reaction process at optimal temperature and synthesis reactor | |
| CN102872767B (en) | Industrialized plate type reactor for carbonylating and coupling to synthesize ester | |
| CN207716869U (en) | A kind of horizontal smelting vacuum furnace device | |
| CN105833804A (en) | Steam rising type radial-flow reactor | |
| CN100386138C (en) | Internal heat exchange catalytic reaction method and equipment | |
| CN2048064U (en) | Internal construction member of cocurrent flow gas-distributing ammonia synthetic tower | |
| US4263260A (en) | High pressure and high temperature heat exchanger | |
| CN201971639U (en) | Nitric acid producing oxidation oven with annual output of 300,000 tons of nitric acid | |
| CN110327847B (en) | Radial flow heat exchange fixed bed catalytic reactor | |
| CA1115499A (en) | Apparatus for making carbon black | |
| CN202803218U (en) | Novel low-pressure methanol synthesis tower | |
| CN202876772U (en) | Industrialized plate type reactor for synthesizing ester by carbonylation coupling | |
| US11718535B1 (en) | Ammonia synthesis converter and method for small production units | |
| CN2680348Y (en) | Internal Heat Exchange Catalytic Reactor | |
| CN206553480U (en) | Coke-stove gas multistage integral type isothermal methanation reactor | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN2290400Y (en) | Improved homogeneous temp gas solid phase cytalytic reactor | |
| CN212492849U (en) | Anti-expansion reactor for preparing ethanol from synthesis gas | |
| CN210560165U (en) | Methanol synthesis system | |
| CN205635893U (en) | Carbon fiber continuous production activation furnace | |
| CN223069476U (en) | Temperature-controlled reactor suitable for methylamine synthesis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |