CN105651082A - Series combining method for siphoning type pasty material heat exchangers - Google Patents
Series combining method for siphoning type pasty material heat exchangers Download PDFInfo
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- CN105651082A CN105651082A CN201610109972.3A CN201610109972A CN105651082A CN 105651082 A CN105651082 A CN 105651082A CN 201610109972 A CN201610109972 A CN 201610109972A CN 105651082 A CN105651082 A CN 105651082A
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- heat exchanger
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators
- F28F9/262—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators for radiators
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Provided are a series combining method for siphoning type pasty material heat exchangers and a multistage flash evaporation solvent separating method. The material level difference in a process system and barometric pressure energy are utilized, slurry is pushed in a siphoning manner to pass through the multistage series upright n-shaped heat exchangers for convective heat transfer, all stages of flash evaporation material levels are automatically constant, and heat is cyclically utilized. Under the conditions that the total height difference of the material levels is 7.5 m, the density of the slurry is 1,480 kg/m<3>, and the saturated vapor pressure is 40 kPa, the total length of series effective heat transfer pipes is larger than or equal to 48 m, flow velocity in the pipes is larger than or equal to 1.5 m/s, and the heat transfer coefficient is larger than 900 W/m<2>.DEG C. The three-stage series combined n-shaped heat exchangers and flash evaporators connected with the heat exchangers and provided with heat pumps are adopted for carrying out solvent separation on the aqueous solution slurry with the temperature below 100 DEG C, solvent vapor is condensed and recycled, condensation heat is lifted for heat source circulation of the n-shaped heat exchangers through the heat pumps, and the energy consumption of solvent separation is lower than 80 kW/t-water vapor.
Description
Technical field
The present invention relates to pasty material technical field of heat exchange, particularly utilize pasty material self the material level discrepancy in elevation to pass through rainbowInhale the power-economizing method that stream makes many ∩ type heat exchanger tandem compounds.
Background technology
The more employing shell-and-tube heat exchanger of pasty material heat exchange in process industrial, pasty material by pipe in flow withWall convection heat transfer' heat-transfer by convection mode and the outer mobile cleaning fluid Medium Exchange heat of pipe. This type of heat exchanger is in order to prevent pasty material runnerStop up, should make it in pipe, there is higher flow velocity to avoid deposition, not allow have deposition site, institute on heat exchanger structure againMostly be vertical type one way shell-and-tube heat exchanger with pasty material heat exchanger, its heat exchange area be proportional to heat exchanger tube number and pipe range, thisTwo parameters can not be selected arbitrarily by process conditions and heat exchanger specification limits again, therefore when a heat exchanger does not reach techniqueRequire heat exchange area time often take many parallel combinations, every heat exchanger to join a circulating pump, energy consumption and investment with moveCost is proportional increase thereupon also. Make many upright heat exchanger tandem compounds if can overcome pasty material deposition, not onlyCan share a circulating pump, also can utilize the material level discrepancy in elevation of pasty material between the operation of front and back to promote convection heat transfer' heat-transfer by convection without pump, jointCan reduce investment by consumption reduction. Prior art cannot realize the vertical type pasty material heat exchanger tandem compound that utilizes the poor promotion of material level.
Summary of the invention
The present invention discloses a kind of method of hydrocone type pasty material heat exchanger tandem compound, utilizes slurry in process systemThe discrepancy in elevation also for the material level (be slurry level vertical range to common reference plane) of material (hereinafter to be referred as slip) between the operation of front and backBy means of atmosphere pressure energy, siphon promotes slip by convection heat transfer' heat-transfer by convection in the upright ∩ type heat exchanger pipe of many series connection, completes workThe exchange heat task that skill requires. Material level discrepancy in elevation 7.5m, the pulp density 1480kg/m of slip between the operation of front and back3, slipSaturated vapor pressure Ps≤40kPa(absolute pressure) condition under, the ∩ type heat exchanger heat-transfer pipe total length of many series connection is no less than48m, and under the condition without shurry pump the velocity in pipes of can obtain >=1.5m/s.
Mainly invention thought of the present invention is: according to principle of hydrodynamics, the entrance point of ∩ type heat exchanger and the port of export are insertedEnter in the uncovered slurry tank of two different controlling levels, the in the situation that of being full of slip in Tube Sheet of Heat Exchanger, by atmosphere pressure energyThe siphonic effect producing also utilizes entrance point place material level to promote higher than the discrepancy in elevation of port of export place material level, can produce and pass through ∩Serial siphon in type heat exchanger pipe flows, slip from entrance point mouth of pipe vertical lifting flows, crosses ∩ type top, vertical underFalling flows leaves the port of export mouth of pipe, as long as that the discrepancy in elevation of two material levels keeps is certain, velocity in pipes and convection heat transfer' heat-transfer by convection operating mode keepStable, form thus the groundwork unit of a ∩ type heat exchanger, First ∩ type heat exchanger 1 and import thereof as shown in drawingsThe end slurry tank 4 at place and the slurry tank 5 at port of export place. The controlling level of slurry tank 4 is determined by process conditions, slurry tank 5Controlling level reduce h2(m than the controlling level of slurry tank 4), the size of h2 is proportional to flowing of First ∩ type heat exchanger 1Resistance. Within the entrance point of second ∩ type heat exchanger 2 of series connection is also positioned at slurry tank 5, so First ∩ type heat exchanger 1 goes outThe controlling level of mouthful end is the controlling level of second ∩ type heat exchanger 2 entrance point, and the rest may be inferred, except First and, instituteThere is the ∩ type heat exchanger entrance point controlling level of series connection all identical with its last ∩ type heat exchanger port of export controlling level, thusThe serial siphon that forms many ∩ type heat exchanger tandem compounds flows. First ∩ type heat exchanger 1 entrance point place slurry tank 4The controlling level of controlling level and the last ∩ type heat exchanger port of export place slurry tank 7 determines by process conditions, slipThe two controlling level poor of tank 4 and 7, forms many ∩ type heat exchanger tandem compound serial siphons total motive force that flows, shouldMotive force equals slip by the ∩ type heat exchanger flow resistance sum (comprising straight tube resistance and local resistance) of all series connection, each∩ type heat exchanger flow resistance is proportional to again pipe range and (comprises the length of straight pipe of entrance point and the port of export and represent working as of local resistanceAmount length), determine accordingly the total length of many upright ∩ type heat exchanger tandem compounds and the length of each ∩ type heat exchanger separate unit.
As shown in drawings, entrance point and the port of export of upright ∩ type heat exchanger are to have same structure (heat exchanger tube quantity, ruleLattice and stringing mode) fixed tube sheet type shell-and-tube heat exchanger, in pipe, mobile slip is by outer mobile the cleaning of tube wall and pipeFluid media (medium) heat-shift. The upper surface of entrance point and the port of export is positioned at same level and is not more than by one section of radius of curvatureThe ∩ type pipe sealing of 0.8m connects; The slurry level that lower surface is positioned at place slurry tank separately 2.0m at least below. Many straightUnder vertical ∩ type heat exchanger tandem compound continous-stable operating mode,, flow velocity equal by slip flow mobile in each Tube Sheet of Heat ExchangerEqual flow divided by circulation area. Taking second ∩ type heat exchanger 2 shown in accompanying drawing as example, the material of its entrance point place slurry tank 5Slurry averag density ρ2（kg/m3), temperature T2(DEG C), saturated vapor pressure Ps2(Pa), atmospheric pressure Po(Pa), heat exchanger ∩ type topApart from the vertical height H between slurry tank 5 liquid levels2(m) be no more than [(Po－Ps2)/(g·ρ2)-h2/2] calculated value 95%, ifρ2=1480kg/m3、T2=60℃、Ps2=15000Pa、Po=95000Pa、h2=2.5m、g=9.81m/s2(gravity acceleratesDegree), H2≤ 4.05m; Deduction top ∩ type tube connector radius of curvature 0.8m, more than entrance point shell-and-tube heat exchanger exposes liquid levelLength be no more than 3.25m; If its length that stretches into below liquid level is 5.75m, entrance point shell-and-tube heat exchanger length is 9.0m;From symmetry, port of export shell-and-tube heat exchanger length is also taken as 9.0m, and its length that stretches into below slurry tank 6 liquid levels is3.25m, the controlling level of slurry tank 6 reduces h3=2.5m than the controlling level of slurry tank 5; That is: second ∩ type heat exchanger 2Effectively heat exchange length is 18m, and taking the 2.5m material level discrepancy in elevation as motive force, in pipe, pulp flow scooter 1.5m/s is above, heat exchangerHeat transfer coefficient can reach 900W/m2. more than DEG C.
The n platform ∩ type heat exchanger structure of above-mentioned tandem compound is all identical with laying method, according to above method, and every 2.5m material levelThe discrepancy in elevation can promote the ∩ type heat exchanger convection heat transfer' heat-transfer by convection that an effective heat exchange length is 18m, if First entrance point place slipTank 4 is (h2+h3+ with the material level discrepancy in elevation of the last port of export place slurry tank 7 ... + hn)=(L1-Ln), the series connection that can promoteNumber of units n=[(L1-Ln)/2.5] (rounding).
As shown in drawings, auxiliary pump 9 can make slurry circulation in slurry tank by the flash vessel 10 with heat pump, reaches solventThe object that separation and heat recycle.
As shown in drawings, the top of all ∩ type heat exchangers is equipped with the exhaust outlet 11 with seal valve, in heat exchanger importThe lower surface of end and the port of export is all stretched under the condition of the following at least 2.0m of liquid level, and before starting, opening encapsulation valve is bled, untilWhen exhaust outlet is full of liquid, close seal valve, ∩ type heat exchanger can enter siphon flow operating mode under the poor promotion of material level.
Above indication slip, is the mixture of the aqueous solution and SS, wherein solid particulate matter content 1% ~ 40%(mass percent). The material level of the each slurry tank of indication is the vertical range of slurry level to common reference plane.
The invention has the beneficial effects as follows the gravitional force that utilizes atmosphere pressure energy and the poor generation of material level, promote slip and pass through manyThe ∩ type heat exchanger continuous-flow convection heat transfer' heat-transfer by convection of platform series connection, completes cooling, heating and multiple-effect or multistage flash evaporation, contracts than conventional artShort flow process, minimizing power-equipment, saving energy resource consumption.
Appended drawings is hydrocone type pasty material heat exchanger tandem compound method schematic diagram provided by the invention. FigureIn: 1,2,3-∩ type heat exchanger; 4,5,6,7-slurry tank; 8-slurry delivery pump; 9-auxiliary pump; The flash vessel of 10-with heat pump;11-exhaust outlet. Below in conjunction with embodiment, accompanying drawing is further elaborated.
Detailed description of the invention below in conjunction with but be not limited to embodiment and set forth the specific embodiment of the invention
Embodiment 1: slip cooling. This example slip is obtained by mineral processing, its solid particle suspension content 35%(quality percentageNumber), slip averag density 1400kg/m3, in slurry tank 4, its temperature is 95 DEG C, saturated vapor pressure 40kPa(absolute pressure), material levelHighly keep 11.0m. Require before this slip enters delivery pump 8, to be cooled to 80 DEG C, the slip being connected with the import of pump 8The controlling level of tank 7 is not less than 3.0m. It is 860 tons/hour (t/h) that pump 8 is carried the flow of slip.
The convection heat transfer' heat-transfer by convection of 3 ∩ type heat exchanger tandem compounds is set as shown in drawings, between slurry tank 4 and slurry tank 7Heat sink. The structure of 3 ∩ type heat exchangers and size are all identical, and entrance point and port of export shell-and-tube heat exchanger tube side are by 220Root length is that the heat exchanger tube of 9.0m, internal diameter 25mm forms, and slip is by flowing in pipe; In cooling agent and pipe that pipe shell journey is mobileSlip countercurrent heat-transfer, make slip cooling.
Set the length that each ∩ type heat exchanger entrance point stretch into below the slurry tank liquid level of place and be 5.8m, it exposesHeight more than liquid level is 3.2m; The material level discrepancy in elevation of each ∩ type heat exchanger entrance point and port of export place slurry tank is2.5m, under continous-stable operating mode, the last ∩ type heat exchanger 3 port of export place slurry tank 7(are connected with the import of pump 8)Controlling level is 3.5m, meets the technological requirement of pump inlet. Pulp flow in each ∩ type heat exchanger pipe under the poor promotion of this material levelSpeed is all greater than 1.5m/s, and the heat transfer coefficient of heat exchanger is greater than 900W/m2. DEG C. The First ∩ type heat exchanger 1 cooling agent a of series connection80 DEG C of inlet temperatures, 85 DEG C of outlet temperatures, second ∩ type heat exchanger 2 75 DEG C of cooling agent b inlet temperature, 80 DEG C of outlet temperatures,The 3rd ∩ type heat exchanger 3 70 DEG C of cooling agent n inlet temperature, 75 DEG C of outlet temperatures. Under this heat transfer condition, slip is by every∩ type heat exchanger all has the heat of the temperature drop of 5 DEG C, release to be thus equivalent to the heat of vaporization of about 5000kg/h water, by 3 ∩The recuperable Lowlevel thermal energy of slip cooling device of type heat exchanger tandem compound be equivalent to 15t/h water vapour heat, need notAiming at heat exchanger arranges circulating pump, has saved power.
Embodiment 2: slip multistage flash evaporation. This example slip is obtained by mineral processing, its solid particle suspension content 16%(qualityPercentage), slip averag density 1100kg/m3, in slurry tank 4, its temperature is 65 DEG C, saturated vapor pressure 22kPa(absolute pressure),Controlling level keeps 11.0m. Required before entering delivery pump 8 by multistage flash evaporation separating part solvent. The flow of delivery pump 8Be 178 tons/hour (t/h).
Three grades of flash distillations of 3 ∩ type heat exchanger tandem compounds are set as shown in drawings, between slurry tank 4 and slurry tank 7With convection heating system. The structure of 3 ∩ type heat exchangers and size are all identical, and entrance point and port of export shell-and-tube heat exchanger tube side are equalThe heat exchanger tube that is 10.0m, internal diameter 25mm by 62 length forms, and slip is by flowing in pipe; The heating agent that pipe shell journey is mobileFor overcritical organic working medium, mobile slip in countercurrent heat-transfer heating tube.
Set the length that each ∩ type heat exchanger entrance point stretch into below the slurry tank liquid level of place and be 5.0m, it exposesHeight more than liquid level is also 5.0m; The material level discrepancy in elevation of each ∩ type heat exchanger entrance point and port of export place slurry tank is2.5m, under continous-stable operating mode, the last ∩ type heat exchanger 3 port of export place slurry tank 7(are connected with the import of pump 8)Controlling level is 3.5m, and the length that the port of export stretches into below liquid level is that 2.5m(meets at least condition of 2.0m). Poor at this material levelPromote slip flow velocity in lower each ∩ type heat exchanger pipe and be all greater than 1.5m/s, the heat transfer coefficient of heat exchanger is greater than 900W/m2.℃。
70 DEG C of First ∩ type heat exchanger 1 102 DEG C of the heating agent a inlet temperatures of series connection, outlets, adverse current heating slip makes itBe warmed up to 75 DEG C from 65 DEG C; 70 DEG C of second ∩ type heat exchanger 2 100 DEG C of cooling agent b inlet temperature, outlets, adverse current heating slipMake it be warmed up to 74 DEG C from 65 DEG C; 69 DEG C of the 3rd ∩ type heat exchanger 3 98 DEG C of cooling agent n inlet temperature, outlets, adverse current heating materialSlurry makes it be warmed up to 73 DEG C from 64 DEG C. Under this heat transfer condition, the heat that slip absorbs by every ∩ type heat exchanger exceedesThe condensation heat that 2300kg/h water vapour is suitable.
75 DEG C of the slips that First ∩ type heat exchanger 1 heats, by the auxiliary pump being connected with its port of export place slurry tank 59 and flash vessel 10 flash separation solvents, temperature with heat pump drop to be not less than slurry tank 5 65 DEG C of mean temperatures, produce andThe solvent vapo(u)r that ∩ type heat exchanger 1 heating load is suitable, this solvent condenses reclaims, pass through after absorbing this condensation heat by organic working mediumPower is that the heat pump of 180kW is risen to the supercriticality of 102 DEG C, follows as the heating agent a of First ∩ type heat exchanger 1Ring uses, the conversion of its thermic load exceedes 2300kg/h for water vapour condensation number.
By second ∩ type heat exchanger 2 and slurry tank 6 and the auxiliary pump being attached thereto and the flash distillation with heat pump of series connectionDevice realize second level separated from solvent and the 3rd ∩ type heat exchanger 3 by series connection and slurry tank 7 and be attached thereto auxiliaryPump and realize third level separated from solvent with the flash vessel of heat pump, its method and separated from solvent yield all with the first order described in epimereSeparated from solvent reclaims identical, and difference is only that every one-level slurry tank temperature is all than prime low 1 ~ 2 DEG C (reason of heat loss),The operating temperature of heat exchanger and associated equipment is corresponding slightly to change.
The method of this embodiment is applicable to various 100 DEG C of following aqueous solution slip separated from solvent, requires each heat exchangerHeating agent inlet temperature higher more than 20 DEG C than this heat exchanger slurry outlet temperature. Its beneficial effect be utilize atmosphere pressure energy andThe gravitional force of the poor generation of slip material level promotes that three grades of series connection solvent flashings separate and heat recycles, slurry tanks at different levels andThe flash vessel material level autobalance being attached thereto, separating energy consumption, lower than 80kW/t-water vapour, is saved power and operating cost.
The invention is not restricted to above-described embodiment, its technical scheme is explained in summary of the invention part.
Claims (2)
1. a method for hydrocone type pasty material heat exchanger tandem compound, is characterized in that utilizing pasty material in process systemThe material level discrepancy in elevation between the operation of front and back by means of atmosphere pressure energy, promotes slip by the upright ∩ type of many series connection without pumpContinuous-flow convection heat transfer' heat-transfer by convection in Tube Sheet of Heat Exchanger, at slip material level discrepancy in elevation 7.5m, pulp density 1480kg/m3, slip saturated vaporPress Ps≤40kPa(absolute pressure) condition under, the ∩ type heat exchanger heat-transfer pipe total length of many series connection is no less than 48m, slip is at pipeInterior flow velocity >=1.5m/s, the heat transfer coefficient of heat exchanger is greater than 900W/m2.℃；
Entrance point and the port of export of upright ∩ type heat exchanger have same structure (heat exchanger tube quantity, specification and stringing mode)Fixed tube sheet type shell-and-tube heat exchanger, its upper surface is positioned at same level and is not more than the ∩ type of 0.8m by one section of radius of curvaturePipe sealing connects, the slurry level that lower surface is positioned at place slurry tank separately 2.0m at least below; Entrance point place slurry tankMaterial level than the high h(m of material level of port of export place slurry tank), slip averag density ρ (kg/m3), temperature T (DEG C), saturated vaporPress Ps(Pa), atmospheric pressure Po(Pa), the ∩ type top of this heat exchanger apart from vertical between the liquid level of entrance point place slurry tankHeight H (m) is no more than [(Po-Ps)/(g ρ)-h/2] calculated value 95%; Except First and, the ∩ type of all series connectionHeat exchanger entrance point controlling level is all identical with its last port of export controlling level;
Every 2.5m material level discrepancy in elevation can promote ∩ type heat exchanger that an effective heat exchange length is 18m at velocity in pipes >=1.5m/sCondition under convection heat transfer' heat-transfer by convection, all identical ∩ type heat exchanger tandem compounds of n platform structure and laying method, n equals First importThe integer of the value (m) of end place slurry tank material level and the difference of the last port of export place slurry tank material level compared with 2.5m;
All ∩ type heat exchangers top of series connection is equipped with the exhaust outlet with seal valve, and before starting, opening encapsulation valve is bled, straightIn the time that exhaust outlet is full of liquid, close seal valve, heat exchanger can enter siphon flow operating mode; Indication slip is that the aqueous solution is with outstandingThe mixture of floating solid particle, solid particulate matter content 1% ~ 40%(mass percent).
2. a separated from solvent side that adopts hydrocone type pasty material heat exchanger tandem compound to carry out aqueous solution slip multistage flash evaporationMethod, three grades of flash distillations that it is characterized in that arranging 3 ∩ type heat exchanger tandem compounds between two slurry tanks of the poor 7.5m of material level withConvection heating system, slip, by flowing in pipe, flows in the overcritical organic working medium adverse current heating tube that pipe shell journey flowsSlip;
The slip of each ∩ type heat exchanger heating of tandem compound by the auxiliary pump that is connected with its port of export place slurry tank andWith the flash vessel of heat pump realize that solvent flashing separates, slurry temperature drops to the mean temperature, the generation that are not less than this slurry tankSolvent vapo(u)r condensation is reclaimed, is absorbed its condensation heat and by heat pump, organic working medium risen to than this ∩ type heat exchange by organic working mediumThe high 20 DEG C of above supercriticalities of device slurry outlet temperature, recycle as the heating agent of this heat exchanger;
The separated from solvent yields at different levels of tandem compound are identical; Every one-level slurry tank temperature is lower 1 ~ 2 DEG C than prime;
The separation process of aqueous solution slip solvent flashing is carried out below at 100 DEG C; Slurry tanks at different levels and the flash vessel being attached thereto thereofMaterial level autobalance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610109972.3A CN105651082B (en) | 2016-02-29 | 2016-02-29 | Hydrocone type pasty material heat exchanger tandem compound method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610109972.3A CN105651082B (en) | 2016-02-29 | 2016-02-29 | Hydrocone type pasty material heat exchanger tandem compound method |
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| CN105651082A true CN105651082A (en) | 2016-06-08 |
| CN105651082B CN105651082B (en) | 2017-08-04 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3898961A (en) * | 1972-06-26 | 1975-08-12 | Siemens Ag | Steam generator |
| DE3011111A1 (en) * | 1980-03-22 | 1981-10-01 | Willi Dipl.-Volksw. 7560 Gaggenau Bauer | Drain water heat recovery tank - has low-level outlet acting as siphon when flow is heavy |
| JPS59164886A (en) * | 1983-03-10 | 1984-09-18 | Mitsubishi Heavy Ind Ltd | Heat exchanger of shell and tube type |
| WO2001017641A1 (en) * | 1999-09-06 | 2001-03-15 | Ineos Fluor Holdings Limited | Apparatus and method for condensing solvent |
| CN1832979A (en) * | 2003-06-06 | 2006-09-13 | 伊斯曼化学公司 | Polyester process using a pipe reactor |
| CN1968731A (en) * | 2004-02-10 | 2007-05-23 | 得克萨斯A&M大学系统 | Vapor-compression evaporation system and method |
-
2016
- 2016-02-29 CN CN201610109972.3A patent/CN105651082B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3898961A (en) * | 1972-06-26 | 1975-08-12 | Siemens Ag | Steam generator |
| DE3011111A1 (en) * | 1980-03-22 | 1981-10-01 | Willi Dipl.-Volksw. 7560 Gaggenau Bauer | Drain water heat recovery tank - has low-level outlet acting as siphon when flow is heavy |
| JPS59164886A (en) * | 1983-03-10 | 1984-09-18 | Mitsubishi Heavy Ind Ltd | Heat exchanger of shell and tube type |
| WO2001017641A1 (en) * | 1999-09-06 | 2001-03-15 | Ineos Fluor Holdings Limited | Apparatus and method for condensing solvent |
| CN1832979A (en) * | 2003-06-06 | 2006-09-13 | 伊斯曼化学公司 | Polyester process using a pipe reactor |
| CN1968731A (en) * | 2004-02-10 | 2007-05-23 | 得克萨斯A&M大学系统 | Vapor-compression evaporation system and method |
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| CN105651082B (en) | 2017-08-04 |
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Granted publication date: 20170804 Termination date: 20190228 |